Polymer recyclate processes and products

ABSTRACT

Methods for processing polyolefin recyclates including, but not limited to, polyethylene and polypropylene and compositions therefrom are provided. polyolefin recyclate feedstocks can be visbroken to improve processing characteristics and/or devolatilized to remove waste byproducts to produce processed polyolefin recyclates. Processed polyolefin recyclates are compounded with pre-consumer polyolefins to produce blend compositions having acceptable or even improved processing characteristics. Such pre-consumer polyolefins can also be visbroken to further tailor processing characteristics of such polymer blends. A combination of extruders and/or extruder zones can be used at the same or different locations for visbreaking and/or compounding of both polyolefin recyclate and/or pre-consumer polyolefins.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the priority of U.S. Provisional Patent Application Ser. No. 63/213,429, entitled “POLYMER RECYCLATE PROCESSES AND PRODUCTS,” filed on Jun. 22, 2021, and U.S. Provisional Patent Application Ser. No. 63/238,655, entitled “POLYMER RECYCLATE PROCESSES AND PRODUCTS,” filed on Aug. 30, 2021, the contents of which are incorporated by reference herein in their entirety.

FIELD OF THE INVENTION

The present disclosure relates to the use of extrusion processes to improve the processing characteristics of polyolefin recyclates, either alone or in combination with other polyolefins. The invention further relates to compositions produced by such processes.

BACKGROUND OF THE INVENTION

Polyolefins, including polyethylene and polypropylene, may be used in many applications, including packaging for food and other goods, electronics, automotive components, and a variety of manufactured articles. Waste plastic materials may be obtained from a variety of sources, including differential recovery of municipal plastic wastes that are constituted of flexible packaging (cast film, blown film and BOPP film), rigid packaging, blow molded bottles and injection molded containers. Often, through a step of separation from other polymers, such as PVC, PET or PS, two main polyolefinic fractions may be obtained; namely, polyethylenes (including, HDPE, LDPE, LLDPE) and polypropylenes (including homopolymers, random copolymers, heterophasic copolymers).

The multicomponent nature of the recycled polyolefins or the polyolefinic fractions may result in low mechanical and optical performances of prepared articles or of polyolefin formulations in which part of a virgin polyolefin is replaced by recycled polymer. Unpredictable mechanical and/or optical properties can result from variability of one or more characteristics of the recycled polyolefin including, but not limited to, melt index, high load melt index, melt elasticity, complex viscosity, or combinations thereof. In addition, the recycled polyolefins or the polyolefinic fractions may contain impurities or contamination by other components. Moreover, the molecular weight, the molecular weight distribution and/or the comonomer content of the recycled polyolefins or of the polyolefinic fractions can limit the range of virgin polyolefins into which recycled polyolefins can be incorporated. Another limitation for the use of recycled polyolefins may be the presence of unpleasant odors coming from volatile organic compounds which may have been absorbed in these polymers during their usage.

It may be desirable to separate polyethylene waste into portions which are predominately one or more of HDPE, MDPE, LDPE, LLDPE, or polypropylene. This disclosure provides processes to produce polyolefin compositions comprising recycled polyolefin, such polyolefin compositions having a useful combination of properties. Such disclosed processes may be highly flexible and could be implemented with commonly used equipment and familiar techniques to produce a wide variety of products.

SUMMARY OF THE INVENTION

In general, the present disclosure relates to methods for processing polyolefin recyclates, in particular one or more high density polyethylene (“HDPE”) recyclates, one or more medium density polyethylene (“MDPE”) recyclates, one or more low density polyethylene (“LDPE”) recyclates, one or more low density polyethylene (“LDPE”) recyclates, one or more polypropylene (“PP”) recyclates, or a combination thereor. Such processing includes implementing in an extruder visbreaking conditions to convert a polyolefin recyclate into a visbroken polyolefin recyclate having a reduced weight average molecular weight. In some embodiments, the polyolefin recyclate is also subjected to devolatilization conditions to convert the polyolefin recyclate into a visbroken polyolefin recyclate having a reduced weight average molecular weight and a reduced volatile organic compounds (“VOC”) content.

Visbreaking conditions include thermal visbreaking and/or peroxidation visbreaking. Thermal visbreaking includes temperature, pressure, and mechanical shear sufficient to cause polymer chain scission to predominate over polymer chain branching or crosslinking. Peroxidation visbreaking may occur when a peroxide as added to the polymer melt in an extruder followed by thermal decomposition of the peroxide to form free radicals, which react with the polymer chain to result in chain scission. In some embodiments, visbreaking conditions consist of thermal visbreaking at a temperature at least 180° C. above the melting point of the polyolefin in the absence of, or substantially in the absence, of oxygen.

Devolatilization conditions can include reduction of VOC in a polyolefin by a portion of an extruder having an intensive mixing arrangement and devolatilization sections to enable removal of VOC at high temperatures. Devolatilization conditions can be further enhanced by injection of a gas into the extruder, distribution of the gas in the polymer melt to scavenge VOC components, and extraction of the gas and scavenged VOC components by venting and/or vacuum.

In some embodiments, the processed polyolefin recyclate can be pelletized as a product at the extruder discharge. In other embodiments, the processed polyolefin recyclate can be fed to a second extruder to be compounded or blended with a virgin polyolefin. In yet other embodiments, the virgin polyolefin can be the polyolefin powder product from a polymerization apparatus, a pelletized polyolefin, or the polyolefin melt, which is the product of a third extruder. In any of the embodiments in this paragraph, the virgin polyolefin can have been subjected to a visbreaking process prior to addition to the second reactor.

In some embodiments, virgin polyolefin is fed to a third extruder and the polymer melt form the third extruder is co-fed to the second extruder along with processed polyolefin recyclate melt.

In some embodiments, a composition is provided where the composition is or comprises a polymer blend of from 5 wt. % to 90 wt. % of a polyolefin recyclate and from 10 wt. % to 95 wt. % of a virgin polyolefin, wherein all weight percentages are based on the combined weight of the polymer blend and one or both of the polyolefin recyclate feedstock and the virgin polyolefin are visbroken. Visbreaking can be thermal visbreaking and/or peroxidation visbreaking.

The foregoing has outlined rather broadly the features and technical advantages of the present invention in order that the detailed description of the invention that follows may be better understood. Additional features and advantages of the invention will be described hereinafter, which form the subject matter of the claims of the invention. It should be appreciated by those skilled in the art that the conception and specific embodiments disclosed may be readily utilized as a basis for modifying or designing other film structures and/or processes for carrying out the same purposes of the present invention. It should also be realized by those skilled in the art that such equivalent constructions do not depart from the spirit and scope of the invention as set forth in the appended claims. The novel features which are believed to be characteristic of the invention, both as to its structure and method of manufacture, together with further objects and advantages will be better understood from the following description.

BRIEF DESCRIPTION OF THE FIGURES

The claimed subject matter may be understood by reference to the following description taken in conjunction with the accompanying drawings, in which like reference numerals identify like elements, and in which:

FIG. 1 is a simplified flow diagram of the process to obtain a processed polyolefin recyclate according to embodiments of the invention;

FIG. 2 is simplified flow diagram of the process to obtain a blend of a processed polyolefin recyclate and a virgin polyolefin using two extruders according to embodiments of the invention; and

FIG. 3 is simplified flow diagram of the process to obtain a blend of a processed polyolefin recyclate and a virgin polyolefin using three extruders according to embodiments of the invention.

While the disclosed process and composition are susceptible to various modifications and alternative forms, the drawings illustrate specific embodiments herein described in detail by way of example. It should be understood, however, that the description herein of specific embodiments is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.

DETAILED DESCRIPTION OF THE INVENTION

Illustrative embodiments of the subject matter claimed below will now be disclosed. In the interest of clarity, some features of some actual implementations may not be described in this specification. It will be appreciated that in the development of any such actual embodiments, numerous implementation-specific decisions must be made to achieve the developer's specific goals, such as compliance with system-related and business-related constraints, which will vary from one implementation to another. Moreover, it will be appreciated that such a development effort, even if complex and time-consuming, would be a routine undertaking for those of ordinary skill in the art having the benefit of this disclosure.

The words and phrases used herein should be understood and interpreted to have a meaning consistent with the understanding of those words and phrases by those skilled in the relevant art. No special definition of a term or phrase, i.e., a definition that is different from the ordinary and customary meaning as understood by those skilled in the art, is intended to be implied by consistent usage of the term or phrase herein. To the extent that a term or phrase is intended to have a special meaning, i.e., a meaning other than the broadest meaning understood by skilled artisans, such a special or clarifying definition will be expressly set forth in the specification in a definitional manner that provides the special or clarifying definition for the term or phrase. It must also be noted that, as used in the specification and the appended claims, the singular forms “a,” “an,” and “the” include plural references unless otherwise specified.

For example, the following discussion contains a non-exhaustive list of definitions of several specific terms used in this disclosure (other terms may be defined or clarified in a definitional manner elsewhere herein). These definitions are intended to clarify the meanings of the terms used herein. It is believed that the terms are used in a manner consistent with their ordinary meaning, but the definitions are nonetheless specified here for clarity.

Definitions

“Antioxidant agents,” as used herein, means compounds that inhibit oxidation, a chemical reaction that can produce free radicals and chain reactions.

“Compounding conditions,” as used herein, means temperature, pressure, and shear force conditions implemented in an extruder to provide intimate mixing of two or more polymers and optionally additives to produce a substantially homogeneous polymer product.

“Devolatilization conditions,” as used herein, means subjecting a polymer melt in an extruder to injection and withdrawal of a scavenging gas, addition of heat, physical mixing, pressure reduction by venting or applying vacuum, or a combination thereof. Devolatilization conditions implemented in an extruder are sufficient to reduce the VOC of a polymer fed to the extruder by a predetermined percentage and/or to a predetermined VOC target for polymer exiting the extruder. Devolatilization conditions are directed to reduction of VOC in a polyolefin by a portion of an extruder having an intensive mixing arrangement and devolatilization sections to enable removal of VOC at high temperatures. Devolatilization conditions can be further enhanced by injection of a gas into the extruder, distribution of the gas in the polymer melt to scavenge VOC components, and extraction of the gas and scavenged VOC components by venting or vacuum.

“Devolatilized polyolefin recyclate,” as used herein, means the product obtained by subjecting an polyolefin recyclate feedstock to devolatilization conditions as described herein.

“Extruder,” as used herein within the context of the “first extruder,” second extruder,” and “third extruder,” in some embodiments, means separate extrusion apparatuses, and in other embodiments, means separate sections within a single extrusion apparatus. In some embodiments, the first extruder and the second extruder are separate machines. In some embodiments, the first extruder and the second extruder are separate sections in a single machine. In some embodiments, the second extruder and the third extruder are separate machines. In some embodiments, the second extruder and the third extruder are separate sections in a single machine. In some embodiments, the first extruder, the second extruder, and the third extruder are separate machines. In some embodiments, the first extruder, the second extruder, and the third extruder are separate sections in a single machine. “Extruder,” as used herein includes any device or combinations of devices capable of continuously processing one or more polyolefins under visbreaking conditions, compounding conditions, melting conditions, or devolatilization conditions, including, but not limited to, Farrel continuous mixers (FCM™ mixers, available from Farrel Corporation, Ansonia, Conn.).

“HDPE,” as used herein, means ethylene homopolymers and ethylene copolymers produced in a gas phase and/or slurry phase polymerization and having a density in the range of 0.940 g/cm³ to 0.970 g/cm³.

“Polyolefin recyclate feedstock,” as used herein, means polyolefin recyclate after collection and sorting but prior to being subjected to the processes disclosed herein.

“Polyolefin recyclate,” as used herein, means post-consumer recycled (“PCR”) polyolefin and/or post-industrial recycled (“PIR”) polyolefin. Polyolefin recyclate is derived from an end product that has completed its life cycle as a consumer item and would otherwise be disposed of as waste (e.g., a polyethylene water bottle) or from plastic scrap that is generated as waste from an industrial process. Post-consumer polyolefins include polyolefins that have been collected in commercial and residential recycling programs, including flexible packaging (cast film, blown film and BOPP film), rigid packaging, blow molded bottles, and injection molded containers. Usually, through a step of separation from other polymers, such as PVC, PET or PS, two main polyolefinic fractions are obtained, namely polyethylene recyclate (including HDPE, MDPE, LDPE, and LLDPE) and polypropylene recyclate (including homopolymers, random copolymers, and heterophasic copolymers). Polyethylene recyclate can be further separated to recover a portion having polyolefin as the primary constituent. In addition to contamination from dissimilar polymers, polyolefin recyclate frequently contains other impurities such as PMMA, PC, wood, paper, textile, cellulose, food, and other organic wastes, many of which cause the polyolefin recyclate to have an unpleasant odor before and after typical processing.

“LDPE,” as used herein, means ethylene homopolymers and ethylene copolymers produced in a high pressure free radical polymerization and having a density in the range of 0.910 g/cm³ to 0.940 g/cm³.

“LLDPE,” as used herein, means ethylene copolymers produced in a gas phase and/or slurry phase polymerization and having a density in the range of 0.910 g/cm³ to 0.940 g/cm³.

“MDPE,” as used herein, means ethylene copolymers produced in a gas phase and/or slurry phase polymerization and having a density in the range of 0.925 g/cm³ to 0.940 g/cm³.

“Melting conditions,” as used herein, means temperature, pressure, and shear force conditions, either alone or in combination with one another, that are required to produce a polymer melt from a feed of polymer pellets or powder.

“Processed polyolefin recyclate,” as used herein, means the product obtained by subjecting an polyolefin recyclate feedstock to visbreaking conditions or to visbreaking conditions followed by devolatilization conditions, as described herein.

“Virgin polyolefins,” as used herein, are pre-consumer polyolefins. Pre-consumer polyolefins are polyolefin products obtained directly or indirectly from petrochemical feedstocks fed to a polymerization apparatus. Pre-consumer polyolefins can be subjected to post polymerization processes such as, but not limited to, extrusion, pelletization, visbreaking, and/or other processing completed before the product reaches the end-use consumer. In some embodiments, virgin polyolefins have a single heat history. In some embodiments, virgin polyolefins have more than one heat history. In some embodiments, virgin polyolefins comprise no additives. In some embodiments, virgin polyolefins comprise additives.

“Visbreaking conditions,” as used herein, means thermal visbreaking and/or peroxidation visbreaking. Thermal visbreaking includes temperature, pressure, and/or mechanical shear sufficient to cause polymer chain scission to predominate of polymer chain branching or crosslinking. Peroxidation visbreaking occurs when a peroxide as added to the polymer melt in an extruder followed by thermal decomposition of the peroxide to form free radicals, which react with the polymer chain to result in chain scission. As used herein, a polymer that has been visbroken will have lower number average and weight average molecular weight, a narrower molecular weight distribution, higher melt index, and a higher high load melt index. In some embodiments, visbreaking conditions consist of thermal visbreaking at a temperature greater than or equal to 300° C., or in the range of from 320° C. to 400° C., in the absence of or substantially in the absence of oxygen.

“Visbreaking,” as used herein, means treating a polymer thermally and/or chemically to produce a reduction in M_(n), M_(w), and MWD (M_(w)/M_(n)), and an increase in melt index I₂ (ASTM D-1238, 2.16 kg @ 190° C.) and high load melt index I₂₁ (ASTM D-1238, 21.6 kg @ 190° C.) of the polyolefin so treated. Applying high temperatures and/or adding radical source such as peroxides to polyolefinic materials results in degradation of the polymer chains and reduction of the average molecular weight of the polymer. In parallel, the molecular weight distribution gets narrower. When intentionally performing such methods for modifying the properties of polymers, these practices are commonly called “visbreaking”.

“Visbroken polyolefin recyclate,” as used herein, means the product obtained by subjecting an polyolefin recyclate feedstock to visbreaking conditions as described herein.

Processing Polyolefin Recyclate Feedstock

In FIG. 1 , flow diagram 100 includes a visbreaking extruder 110 having a visbreaking zone 115 and an optional devolatilization zone 120. Polyolefin recyclate feedstock 125 is added to visbreaking extruder 110 proximate to the inlet end of the extruder. The polyolefin recyclate is drawn through the extruder 110 by one or more rotating screw drives in the barrel of the visbreaking extruder 110. The length of the visbreaking extruder 110 is separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, inlets for injection of gas 130, 135, vents or vacuum connections for withdrawal of gas 140, means for addition or withdrawal of heat, inlets for injection of peroxide 145, and inlets for injection of additives in order to impart preselected process conditions including, but not limited to pressure, temperature, and/or shear force.

FIG. 1 shows an embodiment with both a visbreaking zone 115 and an optional devolatilization zone 120. Other embodiments can have a visbreaking zone 115 alone without a devolatilization zone. Process conditions in the visbreaking extruder 110 can further be controlled by rotation speed of the screw drive. Processed polyolefin recyclate 150 is withdrawn proximate to the discharge of the visbreaking extruder 110 for further processing or pelletization.

HDPEs and/or MDPEs

HDPEs and/or MDPEs comprise homopolymers, copolymers of units derived from ethylene and units derived from one or more of C₃-C₁₂ α-olefins, copolymers of units derived from ethylene and units derived from one or more of alpha mono-olefins. Such C₃-C₁₂ α-olefins include, but are not limited to, substituted or unsubstituted C₃ to C₁₂ alpha olefins such as propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecane, and isomers thereof. When present, comonomers can be present in amounts up to 20 wt %, 15 wt %, 10 wt %, or 5 wt %.

Such ethylene homopolymers and/or copolymers can be produced in a suspension, solution, slurry, or gas phase process, using known equipment and reaction conditions. In some embodiments, polymerization temperatures range from about 0° C. to about 300° C. at atmospheric, subatmospheric, or superatmospheric pressures.

Slurry or solution polymerization systems can utilize subatmospheric or superatmospheric pressures and temperatures in the range of about 40° C. to about 300° C. An exemplary liquid phase polymerization system is described in U.S. Pat. No. 3,324,095, the disclosure of which is fully incorporated by reference herein. Liquid phase polymerization systems generally comprise a reactor to which olefin monomer and catalyst composition are added, and which contains a liquid reaction medium for dissolving or suspending the polyolefin. The liquid reaction medium may consist of the bulk liquid monomer or an inert liquid hydrocarbon that is nonreactive under the polymerization conditions employed. Although such an inert liquid hydrocarbon need not function as a solvent for the catalyst composition or the polymer obtained by the process, it usually serves as solvent for the monomers employed in the polymerization. Among the inert liquid hydrocarbons suitable for this purpose are isopentane, hexane, cyclohexane, heptane, benzene, toluene, and the like. Reactive contact between the olefin monomer and the catalyst composition should be maintained by constant stirring or agitation. The reaction medium containing the olefin polymer product and unreacted olefin monomer is withdrawn from the reactor continuously. The olefin polymer product is separated, and the unreacted olefin monomer and liquid reaction medium are recycled into the reactor.

Gas phase polymerization systems can utilize superatmospheric pressures in the range of from 1 psig (6.9 kPag) to 1,000 psig (6.9 MPag), 50 psig (344 kPag) to 400 psig (2.8 MPag), or 100 psig (689 kPag) to 300 psig (2.1 MPag), and temperatures in the range of from 30° C. to 130° C. or 65° C. to 110° C. Gas phase polymerization systems can be stirred or fluidized bed systems. In some embodiments, a gas phase, fluidized bed process is conducted by passing a stream containing one or more olefin monomers continuously through a fluidized bed reactor under reaction conditions and in the presence of catalyst composition at a velocity sufficient to maintain a bed of solid particles in a suspended condition. A stream containing unreacted monomer is withdrawn from the reactor continuously, compressed, cooled, optionally partially or fully condensed, and recycled into the reactor. Product is withdrawn from the reactor and make-up monomer is added to the recycle stream. As desired for temperature control of the polymerization system, any gas inert to the catalyst composition and reactants may also be present in the gas stream.

In some embodiments, a catalyst based on a Group VIB metal is used. In some embodiments the catalyst is a chromium-based catalyst. Such HDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.940 g/cm³ to 0.970 g/cm³. Such MDPE copolymers have some long-chain branching and a density in the range of from 0.925 g/cm³ to 0.940 g/cm³.

In some embodiments, a Ziegler-Natta (ZN)catalyst is used. Such catalysts are based on a Group IVB transition metal compound and an organoaluminum compound (co-catalyst). Such transition metals, include, but not limited to, Ti, Zr, and Hf. Nonlimiting examples of ZN catalyst systems include TiCl₄+Et₃Al and TiCl₃+AlEt₂Cl. Such HDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.940 g/cm³ to 0.970 g/cm³.

LLDPEs

LLDPEs comprise ethylene homopolymers, copolymers of units derived from ethylene and units derived from one or more of C₃-C₁₂ α-olefins, copolymers of units derived from ethylene and units derived from one or more of alpha mono-olefins. Such C₃-C₁₂ α-olefins include, but are not limited to, substituted or unsubstituted C₃ to C₁₂ alpha olefins such as propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecane, and isomers thereof. When present, comonomers can be present in amounts up to 20 wt %, 15 wt %, 10 wt %, or 5 wt %. Such ethylene homopolymers and/or copolymers can be produced in a suspension, solution, slurry, or gas phase process, using known equipment and reaction conditions. In some embodiments, polymerization temperatures range from about 0° C. to about 300° C. at atmospheric, subatmospheric, or superatmospheric pressures.

Slurry or solution polymerization systems can utilize subatmospheric or superatmospheric pressures and temperatures in the range of about 40° C. to about 300° C. An exemplary liquid phase polymerization system is described in U.S. Pat. No. 3,324,095, the disclosure of which is fully incorporated by reference herein. Liquid phase polymerization systems generally comprise a reactor to which olefin monomer and catalyst composition are added, and which contains a liquid reaction medium for dissolving or suspending the polyolefin. The liquid reaction medium may consist of the bulk liquid monomer or an inert liquid hydrocarbon that is nonreactive under the polymerization conditions employed. Although such an inert liquid hydrocarbon need not function as a solvent for the catalyst composition or the polymer obtained by the process, it usually serves as solvent for the monomers employed in the polymerization. Among the inert liquid hydrocarbons suitable for this purpose are isopentane, hexane, cyclohexane, heptane, benzene, toluene, and the like. Reactive contact between the olefin monomer and the catalyst composition should be maintained by constant stirring or agitation. The reaction medium containing the olefin polymer product and unreacted olefin monomer is withdrawn from the reactor continuously. The olefin polymer product is separated, and the unreacted olefin monomer and liquid reaction medium are recycled into the reactor.

Gas phase polymerization systems can utilize superatmospheric pressures in the range of from 1 psig (6.9 kPag) to 1,000 psig (6.9 MPag), 50 psig (344 kPag) to 400 psig (2.8 MPag), or 100 psig (689 kPag) to 300 psig (2.1 MPag), and temperatures in the range of from 30° C. to 130° C. or 65° C. to 110° C. Gas phase polymerization systems can be stirred or fluidized bed systems. In some embodiments, a gas phase, fluidized bed process is conducted by passing a stream containing one or more olefin monomers continuously through a fluidized bed reactor under reaction conditions and in the presence of catalyst composition at a velocity sufficient to maintain a bed of solid particles in a suspended condition. A stream containing unreacted monomer is withdrawn from the reactor continuously, compressed, cooled, optionally partially or fully condensed, and recycled into the reactor. Product is withdrawn from the reactor and make-up monomer is added to the recycle stream. As desired for temperature control of the polymerization system, any gas inert to the catalyst composition and reactants may also be present in the gas stream.

In some embodiments, a Ziegler-Natta (ZN) catalyst is used. Such catalysts are based on a Group IVB transition metal compound and an organoaluminum compound (co-catalyst). Such transition metals, include, but not limited to, Ti, Zr, and Hf Nonlimiting examples of ZN catalyst systems include TiCl₄+Et₃Al and TiCl₃+AlEt₂Cl. Such LLDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.910 g/cm³ to 0.940 g/cm³.

LDPEs

LLDPEs comprise ethylene homopolymers, copolymers of units derived from ethylene and units derived from one or more of C₃-C₁₂ α-olefins, copolymers of units derived from ethylene and units derived from one or more of alpha mono-olefins comprising polar groups, or mixtures thereof.

Such ethylene homopolymers can be produced in a high pressure, free-radical polymerization process, such as in one or more tubular reactors, one or more autoclave reactors, or a combination thereof. Operating conditions for the high-pressure process can include, but are not limited to, a pressure in the range of from 70 MPa to 700 MPa and a temperature in the range of from 150° C. to 500° C. Such homopolymers have a high degree of long-chain branching and a density in the range of from 0.910 g/cm³ to 0.940 g/cm³.

Such copolymers of ethylene and C₃-C₁₂ α-olefins can be produced in a high pressure, free-radical polymerization process, such as in one or more tubular reactors, one or more autoclave reactors, or a combination thereof. Such C₃-C₁₂ α-olefins include, but are not limited to, substituted or unsubstituted C₃ to C₁₂ alpha olefins such as propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecane, and isomers thereof. When present, comonomers can be present in amounts up to 15 wt %, 10 wt %, or 5 wt %. Operating conditions for the high-pressure process can include, but are not limited to, a pressure in the range of from 70 MPa to 700 MPa and a temperature in the range of from 150° C. to 500° C. Such homopolymers have a high degree of long-chain branching and a density in the range of from 0.910 g/cm³ to 0.940 g/cm³.

Such copolymers of ethylene and one or more of alpha mono-olefins comprising polar groups can be produced in a high pressure, free-radical polymerization process, such as in one or more tubular reactors, one or more autoclave reactors, or a combination thereof. Such alpha mono-olefins comprising polar groups include, but are not limited to, methacrylic acids, esters, nitriles, and amides, such as acrylic acid, methacrylic acid, cyclohexyl methacrylate, methyl acrylate, acrylonitrile, acrylamide, or mixtures thereof. When present, comonomers can be present in amounts up to 15 wt %, 10 wt %, or 5 wt %. Operating conditions for the high-pressure process can include, but are not limited to, a pressure in the range of from 70 MPa to 700 MPa and a temperature in the range of from 150° C. to 500° C. Such homopolymers have a high degree of long-chain branching and a density in the range of from 0.910 g/cm³ to 0.940 g/cm³.

Polypropylenes

Polypropylenes comprise propylene homopolymers and copolymers of units derived from propylene and units derived from one or more of ethylene and C₄-C₁₂ α-olefins. Polypropylenes can be homopolymers, heterophasic copolymers, random copolymers, and combinations thereof.

Polyolefin Recyclate Feedstock

In some embodiments, polyolefin recyclate feedstock is derived from one or more HDPEs, one or more MDPEs, one or more LDPEs, one or more LLDPEs, one or more PPs, or a combination thereof. Polyolefin recyclate feedstock, derived from HDPE, MDPE, LLDPE, LDPE, PP, as described above, or combinations thereof can be characterized by having:

-   -   i) a density in the range of from 0.900 g/cm³ to 0.970 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) less than or equal to         5.0 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         4.0 or greater than 5.0;     -   iv) a weight average molecular weight greater than or equal to         85,000 daltons, greater than or equal to 100,000 daltons,         greater than or equal to 150,000 daltons, greater than or equal         to 200,000 daltons, or greater than or equal to 250,000 daltons,         and/or less than or equal to 600,000 daltons, less than or equal         to 500,000 daltons, less than or equal to 400,000 daltons, or         less than or equal to 300,000 daltons; and     -   v) a melt elasticity (ER) greater than or equal to 0.5.

In some embodiments, in addition to the foregoing properties, the polyolefin recyclate feedstock can be further characterized by having one or more of:

-   -   vi) a first VOC content;     -   vii) a first high load melt index (I₂₁; 21.6 kg, 190° C.;     -   viii) a first melt index ratio (MIR, I₂₁/I₂);     -   ix) a first long chain branching parameter (g′) less than or         equal to 1.0, 0.99, 0.98, 0.97;     -   x) a first overall polydispersity ratio (PDR);     -   xi) a first complex viscosity ratio (η*_(0.1)/η*₁₀₀); and     -   xii) a first intrinsic viscosity.

Visbreaking Extruder

Polyolefin recyclate feedstock is fed to a first extruder and is subjected to visbreaking conditions and optionally devolatilization conditions.

Visbreaking

Visbreaking conditions are implemented in the visbreaking zone of the first extruder and are tailored for polyolefins. In some embodiments, visbreaking conditions means thermal visbreaking and/or peroxidation visbreaking. In some embodiments, visbreaking conditions consist of thermal visbreaking, wherein the temperature in the visbreaking zone is greater than or equal to 300° C., where it is believed that chain scission reactions exceed long-chain branching and/or crosslinking reactions. In some embodiments, temperatures in the visbreaking zone can be in the range of from 320° C. to 500° C., from 340° C. to 480° C., or from 360° C. to 460° C. In some embodiments, instrumentation at the first extruder discharge monitors rheology directly or indirectly (I₂, I₂₁, viscosity, melt elasticity, complex viscosity ratio, or the like) to measure and assist in control of visbreaking. In some embodiments, where antioxidant addition is used in conjunction with visbreaking, the antioxidant addition point is at a location on the first extruder after a substantial portion of the visbreaking reaction has taken place. In some embodiments, visbreaking conditions consist of thermal visbreaking the absence of or substantially in the absence of oxygen, wherein substantial absence of oxygen means less than or equal to 1.0 wt %, less than or equal to 0.10 wt %, or less than or equal to 0.01 wt %, based on the total weight of polymer in the extruder. In some embodiments, the visbreaking extruder comprises one or more melt filters.

Devolatilization

Devolatilization conditions are optionally implemented in the first extruder and are directed to reduction of VOC in the polyolefin recyclate feedstock by a portion of an extruder having an intensive mixing arrangement and devolatilization sections to enable removal of VOC at high temperatures. Devolatilization conditions can be further enhanced by: injection of a scavenging gas, such as, but not limited to, nitrogen, carbon-dioxide, water, or combinations thereof, into the extruder; distribution of the gas in the polymer melt to scavenge VOC components; and extraction of the gas and scavenged VOC components by venting and/or vacuum.

Processed Polyolefin Recyclate

A processed polyolefin recyclate is withdrawn from the discharge of the visbreaking extruder, wherein “processed” means that the polyolefin recyclate feedstock was subjected to visbreaking conditions or visbreaking conditions followed by devolatilization conditions. Processed polyolefin recyclate, as described above, can be characterized by having:

-   -   i) a density, wherein the ratio of the density of the processed         polyolefin recyclate to the density of the polyolefin recyclate         feedstock is greater than or equal to 1.0;     -   ii) a melt index, wherein the ratio of the melt index of the         processed polyolefin recyclate to the melt index of the         polyolefin recyclate feedstock is greater than or equal to 5.0         and/or the melt index of the processed polyolefin recyclate is         greater than or equal to 5.0 g/10 min. or greater than or equal         to 10.0 g/10 min.;     -   iii) a molecular weight distribution, wherein the ratio of         molecular weight distribution of the processed polyolefin         recyclate to the molecular weight distribution of the polyolefin         recyclate feedstock is in the range of from 0.25 to 0.60, from         0.30 to 0.55, or from 0.35 to 0.50;     -   iv) a weight average molecular weight (“M_(w2)”), wherein the         ratio of the weight average molecular weight of the processed         polyolefin recyclate to the weight average molecular weight of         the polyolefin recyclate feedstock is in the range of from 0.10         to 0.70, from 0.15 to 0.60, or from 0.20 to 0.50; and     -   v) a melt elasticity (“ER”), wherein the ratio of the ER of the         processed polyolefin recyclate to the ER of the polyolefin         recyclate feedstock is in the range of from 0.10 to 0.45, from         0.15 to 0.40, or from 0.20 to 0.35, and/or the second melt         elasticity is less than or equal to 2.0, less than or equal to         1.5, or less than or equal to 1.3, and/or greater than or equal         to 0.75, greater than or equal to 0.85, or greater than or equal         to 0.95.

In some embodiments, in addition to the foregoing properties, the processed polyolefin recyclate can be further characterized by having one or more of:

-   -   vi) a VOC content, wherein the ratio of the VOC content of the         processed polyolefin recyclate to the VOC content of the         polyolefin recyclate feedstock is less than or equal to 0.9,         0.8, 0.7, 0.6, or 0.5, each alone or in combination with a lower         limit of greater than or equal to 0.1;     -   vii) a high load melt index (I₂₁; 21.6 kg, 190° C.), wherein the         ratio of the high load melt index of the processed polyolefin         recyclate to the high load melt index of the polyolefin         recyclate feedstock is greater than or equal to 2.0, greater         than or equal to 3.0, or greater than or equal to 4.0;     -   viii) a melt index ratio (MIR, I₂₁/I₂), wherein the MIR of the         processed polyolefin recyclate to the MIR of the polyolefin         recyclate feedstock is in the range of from 0.30 to 0.60;     -   ix) a long chain branching parameter (g′), wherein the ratio of         the g′ of processed polyolefin recyclate to the g′ of the         polyolefin recyclate feedstock is less than or equal to 1.0;     -   x) a first long chain branching index (“LCBI”) greater than or         equal to 0.60, and the processed polyolefin recyclate has a LCBI         less than or equal to 0.40;     -   xi) an overall polydispersity ratio (PDR), wherein the ratio of         the PDR of the processed polyolefin recyclate to the PDR of the         polyolefin recyclate feedstock is less than or equal to 0.50,         less than or equal to 0.45, or less than or equal to 0.40;     -   xii) a complex viscosity ratio (η*_(0.1)/η*₁₀₀), wherein the         ratio of the complex viscosity ratio of the processed polyolefin         recyclate to the complex viscosity ratio of the polyolefin         recyclate feedstock is less than or equal to 0.50, less than or         equal to 0.40, or less than or equal to 0.30, and/or the second         complex viscosity ratio is less than or equal to 10, less than         or equal to 8.0, or less than or equal to 6.0, and η*_(0.1) is         the complex viscosity at 0.1 rad/sec and η*₁₀₀ is the complex         viscosity at 100 rad/sec, both at a temperature of 190° C.; and     -   xiii) an intrinsic viscosity [η], wherein the ratio of the         intrinsic viscosity of the processed polyolefin recyclate to the         intrinsic viscosity of the polyolefin recyclate feedstock is         less than or equal to 0.90, less than or equal to 0.80, or less         than or equal to 0.70.

Blending of Processed Polyolefin Recyclate and a Polyolefin Blend Component—Two Extruders

In FIG. 2 , flow diagram 200 includes a visbreaking extruder 210 and a compounding extruder 255. Embodiments of the present invention as shown in FIG. 2 include a visbreaking extruder 210 having a visbreaking zone 215 and a devolatilization zone 220. polyolefin recyclate feedstock 225 is added to visbreaking extruder 210 proximate to the inlet end of the extruder. The polyolefin recyclate feedstock 225 is drawn through the visbreaking extruder 210 by one or more rotating screw drives in the barrel of the visbreaking extruder 210. The length of the visbreaking extruder 210 is separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, inlets for injection of gas 230, 235, vents or vacuum connections for withdrawal of gas 240, means for addition or withdrawal of heat, inlets for injection of peroxide 245, and inlets for injection of additives in order to impart preselected process conditions including, but not limited to pressure, temperature, and shear force.

FIG. 2 shows an embodiment with both a visbreaking zone 215 and a devolatilization zone 220. Other embodiments can have either a visbreaking zone 215 or a devolatilization zone 220 independently without the other. Process conditions in the visbreaking extruder 210 can further be controlled by rotation speed of the screw drive. Processed polyolefin recyclate 250 is withdrawn proximate to the discharge of the visbreaking extruder 210 for further processing.

Embodiments of FIG. 2 include a second extruder 255, having a compounding zone 260. Processed polyolefin recyclate 250 is added to compounding extruder 255 as a first blend component proximate to the inlet end of the extruder along with a polyolefin blend component 252 and subjected to compounding conditions. The polyolefin blend component 252 comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. In some embodiments, the virgin polyolefin comprises a virgin HDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof. In some embodiments, the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof. In some embodiments, the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed HDPE recyclate, a second processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof. In some embodiments, a polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. The mixture of polyolefin recyclate 250 and polyolefin blend component 252 is drawn through the compounding extruder 255 by one or more rotating screw drives in the barrel of the extruder 255. One or more additional inlets proximate to the inlet end of the extruder provide for the addition of antioxidant agent 265 and/or other components 270. The length of the compounding extruder 255 can be separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, means for addition or withdrawal of heat, inlets for injection of additives. and vents or vacuum connections for withdrawal of gas 275, in order to impart preselected process conditions including, but not limited to pressure, temperature, and shear force. A blend 280 of the processed polyolefin recyclate 250 and the polyolefin blend component 252 is withdrawn proximate to the discharge of the compounding extruder 255 for further processing or pelletization.

In some embodiments, the polyolefin blend component can be a polyolefin powder product from a polymerization apparatus, a pelletized polyolefin, or the polyolefin melt, which is the product withdrawn from a third extruder. In some of these embodiments, the polymerization apparatus comprises two, three, or more polymerization reactors and/or two, three, or more polymerization zones within a polymerization reactor. More specific polymerization apparatus embodiments include, but are not limited to, two or three gas phase fluidized-bed reactors in series, two or three slurry phase reactors in series, and a gas phase fluidized-bed reactor in series with a multizone circulation reactor.

In some embodiments, the amount of the polyolefin blend component, which itself can comprise two or more polymers, is determined based on the logarithmic mixing rule, wherein blend components satisfy the following equation:

${\log\left( {MFR}_{blend} \right)} = {\sum\limits_{i = 1}^{n}\left( {w_{i} \times {\log\left( {MFR}_{i} \right)}} \right)}$

wherein:

-   -   MFR is I₂, I₂₁, or other selected melt index;     -   MFR_(blend) is the target MFR of the final blend product;     -   n is the number of components in the blend; and     -   i is the i-th component of an n-component blend.

Blend Components

A first blend component is a processed polyolefin recyclate produced from a visbreaking extruder. A second blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. In some embodiments, the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin polypropylene, or a combination thereof. In some embodiments, the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof. In some embodiments, the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed polyolefin recyclate, a processed polypropylene recyclate, or a combination thereof. In some embodiments, a polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. When the processed polyolefin recyclate is blended with another processed polyolefin recyclate, the first polyolefin recyclate will have at least one parameter that distinguishes it from the second processed polyolefin recyclate.

Virgin Polyolefin

In some embodiments, virgin polyolefin is derived from ethylene homopolymers, copolymers of units derived from ethylene and units derived from one or more of C₃-C₁₂ α-olefins, copolymers of units derived from ethylene and units derived from one or more of alpha mono-olefins. Such C₃-C₁₂ α-olefins include, but are not limited to, substituted or unsubstituted C₃ to C₁₂ alpha olefins such as propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecane, and isomers thereof. When present, comonomers can be present in amounts up to 20 wt %, 15 wt %, 10 wt %, or 5 wt %. Virgin polyolefin can be derived as a portion of post-consumer recycled polyolefin and/or post-industrial recycled polyolefin that is predominately comprised of polyolefin recyclate, wherein “predominately” means wherein “predominately” means greater than or equal to 80 wt %, greater than or equal to 85 wt %, greater than or equal to 90 wt %, or greater than or equal to 95 wt %, based on the total weight of the virgin polyolefin.

Such ethylene homopolymers and/or copolymers can be produced in a suspension, solution, slurry, or gas phase process, using known equipment and reaction conditions. In some embodiments, polymerization temperatures range from about 0° C. to about 300° C. at atmospheric, subatmospheric, or superatmospheric pressures.

Slurry or solution polymerization systems can utilize subatmospheric or superatmospheric pressures and temperatures in the range of about 40° C. to about 300° C. An exemplary liquid phase polymerization system is described in U.S. Pat. No. 3,324,095, the disclosure of which is fully incorporated by reference herein. Liquid phase polymerization systems generally comprise a reactor to which olefin monomer and catalyst composition are added, and which contains a liquid reaction medium for dissolving or suspending the polyolefin. The liquid reaction medium may consist of the bulk liquid monomer or an inert liquid hydrocarbon that is nonreactive under the polymerization conditions employed. Although such an inert liquid hydrocarbon need not function as a solvent for the catalyst composition or the polymer obtained by the process, it usually serves as solvent for the monomers employed in the polymerization. Among the inert liquid hydrocarbons suitable for this purpose are isopentane, hexane, cyclohexane, heptane, benzene, toluene, and the like. Reactive contact between the olefin monomer and the catalyst composition should be maintained by constant stirring or agitation. The reaction medium containing the olefin polymer product and unreacted olefin monomer is withdrawn from the reactor continuously. The olefin polymer product is separated, and the unreacted olefin monomer and liquid reaction medium are recycled into the reactor.

Gas phase polymerization systems can utilize superatmospheric pressures in the range of from 1 psig (6.9 kPag) to 1,000 psig (6.9 MPag), 50 psig (344 kPag) to 400 psig (2.8 MPag), or 100 psig (689 kPag) to 300 psig (2.1 MPag), and temperatures in the range of from 30° C. to 130° C. or 65° C. to 110° C. Gas phase polymerization systems can be stirred or fluidized bed systems. In some embodiments, a gas phase, fluidized bed process is conducted by passing a stream containing one or more olefin monomers continuously through a fluidized bed reactor under reaction conditions and in the presence of catalyst composition at a velocity sufficient to maintain a bed of solid particles in a suspended condition. A stream containing unreacted monomer is withdrawn from the reactor continuously, compressed, cooled, optionally partially or fully condensed, and recycled into the reactor. Product is withdrawn from the reactor and make-up monomer is added to the recycle stream. As desired for temperature control of the polymerization system, any gas inert to the catalyst composition and reactants may also be present in the gas stream.

In some embodiments, a catalyst based on a Group VIB metal is used. In some embodiments the catalyst is a chromium-based catalyst. Such HDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.940 g/cm³ to 0.970 g/cm³. Such HDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.925 g/cm³ to 0.940 g/cm³.

Virgin HDPE can be characterized by having:

-   -   i) a density in the range of from 0.940 g/cm³ to 0.970 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) in the range of from 1.0         g/10 min. to 100 g/10 min., from 2.0 g/10 min. to 80 g/10 min.,         or from 3.0 g/10 min. to 50 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         15; and     -   iv) a weight average molecular weight less than or equal to         250,000 daltons, less than or equal to 200,000 daltons, less         than or equal to 150,000 daltons, or less than or equal to         100,000 daltons.

Virgin MDPE can be characterized by having:

-   -   i) a density in the range of from 0.925 g/cm³ to 0.940 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) in the range of from 1.0         g/10 min. to 100 g/10 min., from 2.0 g/10 min. to 80 g/10 min.,         or from 3.0 g/10 min. to 50 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         15; and     -   iv) a weight average molecular weight less than or equal to         250,000 daltons, less than or equal to 200,000 daltons, less         than or equal to 150,000 daltons, or less than or equal to         100,000 daltons.

Polyolefin Recyclate Feedstock

In some embodiments, polyolefin recyclate feedstock is derived from one or more HDPEs, one or more MDPEs, one or more LDPEs, one or more LLDPEs, one or more PPs, or a combination thereof. Polyolefin recyclate feedstock, derived from HDPE, MDPE, LLDPE, LDPE, PP, as described above, or combinations thereof can be characterized by having:

-   -   i) a density in the range of from 0.900 g/cm³ to 0.970 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) less than or equal to         5.0 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         4.0 or greater than 5.0;     -   iv) a weight average molecular weight greater than or equal to         85,000 daltons, greater than or equal to 100,000 daltons,         greater than or equal to 150,000 daltons, greater than or equal         to 200,000 daltons, or greater than or equal to 250,000 daltons,         and/or less than or equal to 600,000 daltons, less than or equal         to 500,000 daltons, less than or equal to 400,000 daltons, or         less than or equal to 300,000 daltons; and     -   v) a melt elasticity (ER) greater than or equal to 0.5.

In some embodiments, in addition to the foregoing properties, the polyolefin recyclate feedstock can be further characterized by having one or more of:

-   -   vi) a first VOC content;     -   vii) a first high load melt index (I₂₁; 21.6 kg, 190° C.;     -   viii) a first melt index ratio (MIR, I₂₁/I₂);     -   ix) a first long chain branching parameter (g′) less than or         equal to 1.0, 0.99, 0.98, 0.97;     -   x) a first overall polydispersity ratio (PDR);     -   xi) a first complex viscosity ratio (η*_(0.1)/η*₁₀₀); and     -   xii) a first intrinsic viscosity.

Processed Polyolefin Recyclate

A processed polyolefin recyclate is withdrawn from the discharge of the visbreaking extruder, wherein “processed” means that the polyolefin recyclate feedstock was subjected to visbreaking conditions or visbreaking conditions followed by devolatilization conditions. Processed polyolefin recyclate, as described above, can be characterized by having:

-   -   i) a density, wherein the ratio of the density of the processed         polyolefin recyclate to the density of the polyolefin recyclate         feedstock is greater than or equal to 1.0;     -   ii) a melt index, wherein the ratio of the melt index of the         processed polyolefin recyclate to the melt index of the         polyolefin recyclate feedstock is greater than or equal to 5.0;     -   iii) a molecular weight distribution, wherein the ratio of         molecular weight distribution of the processed polyolefin         recyclate to the molecular weight distribution of the polyolefin         recyclate feedstock is less than or equal to 0.99, less than or         equal to 0.95, or less than or equal to 0.80;     -   iv) a weight average molecular weight (“M_(w2)”), wherein the         ratio of the weight average molecular weight of the processed         polyolefin recyclate to the weight average molecular weight of         the polyolefin recyclate feedstock is less than or equal to         0.99, less than or equal to 0.95, less than or equal to 0.80, or         less than or equal to 0.70; and     -   v) a melt elasticity (“ER”), wherein the ratio of the ER of the         processed polyolefin recyclate to the ER of the polyolefin         recyclate feedstock is less than or equal to 0.90, less than or         equal to 0.70, or less than or equal to 0.50.

In some embodiments, in addition to the foregoing properties, the processed polyolefin recyclate can be further characterized by having one or more of:

-   -   vi) a VOC content, wherein the ratio of the VOC content of the         processed polyolefin recyclate to the VOC content of the         polyolefin recyclate feedstock is less than or equal to 0.9,         0.8, 0.7, 0.6, or 0.5, each alone or in combination with a lower         limit of greater than or equal to 0.1;     -   vii) a high load melt index (I₂₁; 21.6 kg, 190° C.), wherein the         ratio of the high load melt index of the processed polyolefin         recyclate to the high load melt index of the polyolefin         recyclate feedstock is greater than or equal to 2.0, greater         than or equal to 3.0, greater than or equal to 4.0, or greater         than or equal to 5.0;     -   viii) a melt index ratio (MIR, I₂₁/I₂), wherein the MIR of the         processed polyolefin recyclate to the MIR of the polyolefin         recyclate feedstock is less than or equal to 0.90, less than or         equal to 0.85, less than or equal to 0.80, or less than or equal         to 0.75;     -   ix) an overall polydispersity ratio (PDR), wherein the ratio of         the PDR of the processed polyolefin recyclate to the PDR of the         polyolefin recyclate feedstock is less than or equal to 0.90,         less than or equal to 0.80, less than or equal to 0.70, or less         than or equal to 0.50;     -   x) a complex viscosity ratio wherein the ratio of the complex         viscosity ratio of the processed polyolefin recyclate to the         complex viscosity ratio of the polyolefin recyclate feedstock is         less than or equal to 0.70, less than or equal to 0.60, less         than or equal to 0.50, or less than or equal to 0.40; and     -   xi) an intrinsic viscosity [η], wherein the ratio of the         intrinsic viscosity of the processed polyolefin recyclate to the         intrinsic viscosity of the polyolefin recyclate feedstock is         less than or equal to 0.90, less than or equal to 0.80, less         than or equal to 0.70, or less than or equal to 0.50.

Compounding Extruder

Processed polyolefin recyclate and a polyolefin blend component are fed to a second extruder or mixer wherein the blend is subjected to compounding conditions. Compounding conditions are implemented in the compounding zone of the second extruder or mixer and are tailored for mixtures of specific polyolefins and optionally additives. Temperature, pressure, and shear force conditions are implemented in the second extruder or mixer sufficient to provide intimate mixing of the processed polyolefin recyclate and the virgin polyolefin and optionally additives to produce a substantially homogeneous polymer blend of the processed polyolefin recyclate and the virgin polyolefin. In some embodiments, compounding conditions comprise a temperature in the compounding zone of less than or equal to 300° C., less than or equal to 250° C. or less than or equal to 200° C. In some embodiments, temperatures in the compounding zone can be in the range of from 125° C. to 195° C., from 130° C. to 180° C., or from 135° C. to 165° C.

Blends of Processed Polyolefin Recyclate and a Polyolefin Blend Component

In some embodiments, the blend comprises from 5 wt. % to 90 wt. %, 10 wt. % to 80 wt. %, 15 wt. % to 70 wt. %, 20 wt. % to 60 wt. %, or 25 wt. % to 50 wt. %, of a processed polyolefin recyclate and from 10 wt. % to 95 wt. %, 20 wt. % to 90 wt. %, 30 wt. % to 85 wt. %, 40 wt. % to 80 wt. %, or 50 wt. % to 75 wt. %, of a polyolefin blend component, respectively, wherein all weight percentages are based on the combined weight of the polymer blend. In some embodiments, the virgin polyolefin is visbroken. Such visbreaking of virgin polyolefin can be thermal visbreaking and/or peroxidation visbreaking. In some embodiments, such visbreaking conditions for a virgin polyolefin consist of thermal visbreaking at a temperature above the melting point of the polyolefin, greater than or equal to 300° C., or in the range of from 320° C. to 400° C., in the absence of or substantially in the absence of oxygen.

In some embodiments, the blends of processed polyolefin recyclate and a polyolefin blend component, in combination with or independently of the blend ratios in the preceding paragraph, comprise a bimodal polymer, wherein the processed polyolefin recyclate product has a weight average molecular weight (“M_(w3)”), the polyolefin blend component has a weight average molecular weight (“M_(w4)”); and M_(w3)/M_(w4) is either less than or equal to 0.9,0.8, 0.7, 0.6, or 0.5, or alternatively is greater than or equal to 1.1, 1.25, 1.5, 1.75, or 2.0.

Blending of Processed Polyolefin Recyclate and a Polyolefin Blend Component—Three Extruders

In FIG. 3 , flow diagram 300 includes a visbreaking extruder 310, a melting extruder 357, and a compounding extruder 355. Embodiments of the present invention as shown in FIG. 3 include a visbreaking extruder 310 having a visbreaking zone 315 and a devolatilization zone 320. polyolefin recyclate feedstock 325 is added to visbreaking extruder 310 proximate to the inlet end of the extruder. The polyolefin recyclate feedstock 325 is drawn through the visbreaking extruder 310 by one or more rotating screw drives in the barrel of the visbreaking extruder 310. The length of the visbreaking extruder 310 is separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, inlets for injection of gas 330, 335, vents or vacuum connections for withdrawal of gas 340, means for addition or withdrawal of heat, inlets for injection of peroxide 345, and inlets for injection of additives in order to impart preselected process conditions including, but not limited to pressure, temperature, and shear force.

FIG. 3 shows an embodiment with both a visbreaking zone 315 and a devolatilization zone 320. Other embodiments can have either a visbreaking zone 315 or a devolatilization zone 320 independently without the other. Process conditions in the visbreaking extruder 310 can further be controlled by rotation speed of the screw drive. Processed polyolefin recyclate 350 is withdrawn proximate to the discharge of the visbreaking extruder 310 for further processing.

Embodiments of FIG. 3 include a second extruder 355 having a compounding zone 360 and a third extruder 357 having a melting zone 362. A third blend component 383 is added to melting extruder 357 proximate to the inlet end of the extruder optionally along with antioxidant agent 365 and other components 370. The polyolefin blend component 352 comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. In some embodiments, the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof. In some embodiments, the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof. In some embodiments, the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed HDPE recyclate, a second processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof. In some embodiments, a polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. The mixture of third blend component 352 and optional antioxidant 365 and/or other components 370 is drawn through the melting extruder 357 by one or more rotating screw drives in the barrel of the melting extruder 357. The length of the melting extruder 357 can be separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, means for addition or withdrawal of heat, inlets for injection of additives, and vents or vacuum connections for withdrawal of gas, in order to impart preselected process conditions including, but not limited to, pressure, temperature, and shear force. A melt of the polyolefin blend component 352 is withdrawn proximate to the discharge of the melting extruder 357 for further processing or pelletization.

Processed polyolefin recyclate 350 is added to compounding extruder 355 proximate to the inlet end of the extruder along with the melt of the polyolefin blend component 352. The mixture of processed polyolefin recyclate 350 and polyolefin blend component 352 is drawn through the compounding extruder 355 by one or more rotating screw drives in the barrel of the compounding extruder 355 and the mixture is subjected to compounding conditions. The length of the compounding extruder 355 can be separated into one or more zones. Each zone can have one or more of a specified thread pitch on the screw drive, means for addition or withdrawal of heat, inlets for injection of additives, and vents and/or vacuum connections for withdrawal of gas 375, in order to impart preselected process conditions including, but not limited to pressure, temperature, and shear force. A blend 380 of the processed polyolefin recyclate 350 and the polyolefin blend component 352 melt is withdrawn proximate to the discharge of the compounding extruder 355 for further processing or pelletization.

In some embodiments, the polyolefin blend component can be a polyolefin powder product from a polymerization apparatus, a pelletized polyolefin, or the polyolefin melt, which is the product withdrawn from a third extruder. In some of these embodiments, the polymerization apparatus comprises two, three, or more polymerization reactors and/or two, three, or more polymerization zones within a polymerization reactor. More specific polymerization apparatus embodiments include, but are not limited to, two or three gas phase fluidized-bed reactors in series, two or three slurry phase reactors in series, and a gas phase fluidized-bed reactor in series with a multizone circulation reactor.

In some embodiments, the amount of the polyolefin blend component, which itself can comprise two or more polymers, is determined based on the logarithmic mixing rule, wherein blend components satisfy the following equation:

${\log\left( {MFR}_{blend} \right)} = {\sum\limits_{i = 1}^{n}\left( {w_{i} \times {\log\left( {MFR}_{i} \right)}} \right)}$

wherein:

-   -   MFR is I₂, I₂₁, or other selected melt index;     -   MFR_(blend) is the target MFR of the final blend product;     -   n is the number of components in the blend; and     -   i is the i-th component of an n-component blend.

Blend Components

A first blend component is a processed polyolefin recyclate produced from at from a visbreaking extruder. A second blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. In some embodiments, the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof. In some embodiments, the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof. In some embodiments, the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed HDPE recyclate, a second processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof. In some embodiments, the second blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. When the processed polyolefin recyclate is blended with another processed polyolefin recyclate, the first polyolefin recyclate will have at least one parameter that distinguishes it from the second processed polyolefin recyclate.

Virgin Polyolefin

In some embodiments, polyolefin recyclate feedstock is derived from ethylene homopolymers, copolymers of units derived from ethylene and units derived from one or more of C₃-C₁₂ α-olefins, copolymers of units derived from ethylene and units derived from one or more of alpha mono-olefins. Such C₃-C₁₂ α-olefins include, but are not limited to, substituted or unsubstituted C₃ to C₁₂ alpha olefins such as propylene, butene, pentene, hexene, heptene, octene, nonene, decene, undecene, dodecane, and isomers thereof. When present, comonomers can be present in amounts up to 20 wt %, 15 wt %, 10 wt %, or 5 wt %. polyolefin recyclate feedstock can be derived as a portion of post-consumer recycled polyolefin and/or post-industrial recycled polyolefin that is predominately comprised of polyolefin recyclate, wherein “predominately” means wherein “predominately” means greater than or equal to 80 wt %, greater than or equal to 85 wt %, greater than or equal to 90 wt %, or greater than or equal to 95 wt %, based on the total weight of the polyolefin recyclate feedstock.

Such ethylene homopolymers and/or copolymers can be produced in a suspension, solution, slurry, or gas phase process, using known equipment and reaction conditions. In some embodiments, polymerization temperatures range from about 0° C. to about 300° C. at atmospheric, subatmospheric, or superatmospheric pressures.

Slurry or solution polymerization systems can utilize subatmospheric or superatmospheric pressures and temperatures in the range of about 40° C. to about 300° C. An exemplary liquid phase polymerization system is described in U.S. Pat. No. 3,324,095, the disclosure of which is fully incorporated by reference herein. Liquid phase polymerization systems generally comprise a reactor to which olefin monomer and catalyst composition are added, and which contains a liquid reaction medium for dissolving or suspending the polyolefin. The liquid reaction medium may consist of the bulk liquid monomer or an inert liquid hydrocarbon that is nonreactive under the polymerization conditions employed. Although such an inert liquid hydrocarbon need not function as a solvent for the catalyst composition or the polymer obtained by the process, it usually serves as solvent for the monomers employed in the polymerization. Among the inert liquid hydrocarbons suitable for this purpose are isopentane, hexane, cyclohexane, heptane, benzene, toluene, and the like. Reactive contact between the olefin monomer and the catalyst composition should be maintained by constant stirring or agitation. The reaction medium containing the olefin polymer product and unreacted olefin monomer is withdrawn from the reactor continuously. The olefin polymer product is separated, and the unreacted olefin monomer and liquid reaction medium are recycled into the reactor.

Gas phase polymerization systems can utilize superatmospheric pressures in the range of from 1 psig (6.9 kPag) to 1,000 psig (6.9 MPag), 50 psig (344 kPag) to 400 psig (2.8 MPag), or 100 psig (689 kPag) to 300 psig (2.1 MPag), and temperatures in the range of from 30° C. to 130° C. or 65° C. to 110° C. Gas phase polymerization systems can be stirred or fluidized bed systems. In some embodiments, a gas phase, fluidized bed process is conducted by passing a stream containing one or more olefin monomers continuously through a fluidized bed reactor under reaction conditions and in the presence of catalyst composition at a velocity sufficient to maintain a bed of solid particles in a suspended condition. A stream containing unreacted monomer is withdrawn from the reactor continuously, compressed, cooled, optionally partially or fully condensed, and recycled into the reactor. Product is withdrawn from the reactor and make-up monomer is added to the recycle stream. As desired for temperature control of the polymerization system, any gas inert to the catalyst composition and reactants may also be present in the gas stream.

In some embodiments, a catalyst based on a Group VIB metal is used. In some embodiments the catalyst is a chromium-based catalyst. Such HDPE homopolymers and/or copolymers have some long-chain branching and a density in the range of from 0.940 g/cm³ to 0.970 g/cm³. Such MDPE copolymers have some long-chain branching and a density in the range of from 0.925 g/cm³ to 0.940 g/cm³.

Virgin HDPE can be characterized by having:

-   -   i) a density in the range of from 0.940 g/cm³ to 0.970 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) in the range of from 1.0         g/10 min. to 100 g/10 min., from 2.0 g/10 min. to 80 g/10 min.,         or from 3.0 g/10 min. to 50 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         15; and     -   iv) a weight average molecular weight less than or equal to         250,000 daltons, less than or equal to 200,000 daltons, less         than or equal to 150,000 daltons, or less than or equal to         100,000 daltons.

Virgin MDPE can be characterized by having:

-   -   i) a density in the range of from 0.925 g/cm³ to 0.940 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) in the range of from 1.0         g/10 min. to 100 g/10 min., from 2.0 g/10 min. to 80 g/10 min.,         or from 3.0 g/10 min. to 50 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         15; and     -   iv) a weight average molecular weight less than or equal to         250,000 daltons, less than or equal to 200,000 daltons, less         than or equal to 150,000 daltons, or less than or equal to         100,000 daltons.

Polyolefin Recyclate Feedstock

In some embodiments, polyolefin recyclate feedstock is derived from one or more HDPEs, one or more MDPEs, one or more LDPEs, one or more LLDPEs, one or more PPs, or a combination thereof. Polyolefin recyclate feedstock, derived from HDPE, MDPE, LLDPE, LDPE, PP, as described above, or combinations thereof can be characterized by having:

-   -   i) a density in the range of from 0.900 g/cm³ to 0.970 g/cm³;     -   ii) a melt index (I₂; 2.16 kg, 190° C.) less than or equal to         5.0 g/10 min.;     -   iii) a molecular weight distribution (M_(w)/M_(n)) greater than         4.0 or greater than 5.0;     -   iv) a weight average molecular weight greater than or equal to         85,000 daltons, greater than or equal to 100,000 daltons,         greater than or equal to 150,000 daltons, greater than or equal         to 200,000 daltons, or greater than or equal to 250,000 daltons,         and/or less than or equal to 600,000 daltons, less than or equal         to 500,000 daltons, less than or equal to 400,000 daltons, or         less than or equal to 300,000 daltons; and     -   v) a melt elasticity (ER) greater than or equal to 0.5.

In some embodiments, in addition to the foregoing properties, the polyolefin recyclate feedstock can be further characterized by having one or more of:

-   -   vi) a first VOC content;     -   vii) a first high load melt index (I₂₁; 21.6 kg, 190° C.;     -   viii) a first melt index ratio (MIR, I₂₁/I₂);     -   ix) a first long chain branching parameter (g′) less than or         equal to 1.0, 0.99, 0.98, 0.97;     -   x) a first overall polydispersity ratio (PDR);     -   xi) a first complex viscosity ratio (η*_(0.1)/η*₁₀₀); and     -   xii) a first intrinsic viscosity.

Processed Polyolefin Recyclate

A processed polyolefin recyclate is withdrawn from the discharge of the visbreaking extruder, wherein “processed” means that the polyolefin recyclate feedstock was subjected to visbreaking conditions or visbreaking conditions followed by devolatilization conditions. Processed polyolefin recyclate, as described above, can be characterized by having:

-   -   i) a density, wherein the ratio of the density of the processed         polyolefin recyclate to the density of the polyolefin recyclate         feedstock is greater than or equal to 1.0;     -   ii) a melt index, wherein the ratio of the melt index of the         processed polyolefin recyclate to the melt index of the         polyolefin recyclate feedstock is greater than or equal to 5.0;     -   iii) a molecular weight distribution, wherein the ratio of         molecular weight distribution of the processed polyolefin         recyclate to the molecular weight distribution of the polyolefin         recyclate feedstock is less than or equal to 0.99, less than or         equal to 0.95, or less than or equal to 0.80;     -   iv) a weight average molecular weight (“M_(w2)”), wherein the         ratio of the weight average molecular weight of the processed         polyolefin recyclate to the weight average molecular weight of         the polyolefin recyclate feedstock is less than or equal to         0.99, less than or equal to 0.95, less than or equal to 0.80, or         less than or equal to 0.70; and     -   v) a melt elasticity (“ER”), wherein the ratio of the ER of the         processed polyolefin recyclate to the ER of the polyolefin         recyclate feedstock is less than or equal to 0.90, less than or         equal to 0.70, or less than or equal to 0.50.

In some embodiments, in addition to the foregoing properties, the processed polyolefin recyclate can be further characterized by having one or more of:

-   -   vi) a VOC content, wherein the ratio of the VOC content of the         processed polyolefin recyclate to the VOC content of the         polyolefin recyclate feedstock is less than or equal to 0.9,         0.8, 0.7, 0.6, or 0.5, each alone or in combination with a lower         limit of greater than or equal to 0.1;     -   vii) a high load melt index (I₂₁; 21.6 kg, 190° C.), wherein the         ratio of the high load melt index of the processed polyolefin         recyclate to the high load melt index of the polyolefin         recyclate feedstock is greater than or equal to 2.0, greater         than or equal to 3.0, greater than or equal to 4.0, or greater         than or equal to 5.0;     -   viii) a melt index ratio (MIR, I₂₁/I₂), wherein the MIR of the         processed polyolefin recyclate to the MIR of the polyolefin         recyclate feedstock is less than or equal to 0.90, less than or         equal to 0.85, less than or equal to 0.80, or less than or equal         to 0.75;     -   ix) an overall polydispersity ratio (PDR), wherein the ratio of         the PDR of the processed polyolefin recyclate to the PDR of the         polyolefin recyclate feedstock is less than or equal to 0.90,         less than or equal to 0.80, less than or equal to 0.70, or less         than or equal to 0.50;     -   x) a complex viscosity ratio (η*_(0.1)/η*₁₀₀), wherein the ratio         of the complex viscosity ratio of the processed polyolefin         recyclate to the complex viscosity ratio of the polyolefin         recyclate feedstock is less than or equal to 0.70, less than or         equal to 0.60, less than or equal to 0.50, or less than or equal         to 0.40; and     -   xi) an intrinsic viscosity [η], wherein the ratio of the         intrinsic viscosity of the processed polyolefin recyclate to the         intrinsic viscosity of the polyolefin recyclate feedstock is         less than or equal to 0.90, less than or equal to 0.80, less         than or equal to 0.70, or less than or equal to 0.50.

Melting Extruder

The polyolefin blend component and optional antioxidants and/or other components are fed to a third extruder or mixer wherein the blend is subjected to melting conditions. Melting conditions are implemented in the meting zone of the third extruder or mixer and are tailored for mixtures of specific polyolefins and optionally additives. Temperature, pressure, and shear force conditions are implemented in the second extruder or mixer sufficient to provide intimate mixing of the processed polyolefin recyclate and the virgin polyolefin and optionally additives to produce a substantially homogeneous polymer blend of the processed polyolefin recyclate and the virgin polyolefin. In some embodiments, melting conditions comprise a temperature in the melting zone in the range of from 130° C. to 250° C. or from 150° C. to 230° C.

Compounding Extruder

Processed polyolefin recyclate and a polyolefin blend component are fed to a second extruder or mixer wherein the blend is subjected to compounding conditions. Compounding conditions are implemented in the compounding zone of the second extruder or mixer and are tailored for mixtures of specific polyolefins and optionally additives. Temperature, pressure, and shear force conditions are implemented in the second extruder or mixer sufficient to provide intimate mixing of the processed polyolefin recyclate and the virgin polyolefin and optionally additives to produce a substantially homogeneous polymer blend of the processed polyolefin recyclate and the virgin polyolefin. In some embodiments, compounding conditions comprise a temperature in the compounding zone of less than or equal to 300° C., less than or equal to 250° C. or less than or equal to 200° C. In some embodiments, temperatures in the compounding zone can be in the range of from 125° C. to 195° C., from 130° C. to 180° C., or from 135° C. to 165° C.

Blends of Processed Polyolefin Recyclate and a Polyolefin Blend Component

In some embodiments, the blend comprises from 5 wt. % to 90 wt. %, 10 wt. % to 80 wt. %, 15 wt. % to 70 wt. %, 20 wt. % to 60 wt. %, or 25 wt. % to 50 wt. %, of a processed polyolefin recyclate and from 10 wt. % to 95 wt. %, 20 wt. % to 90 wt. %, 30 wt. % to 85 wt. %, 40 wt. % to 80 wt. %, or 50 wt. % to 75 wt. %, of a polyolefin blend component, respectively, wherein all weight percentages are based on the combined weight of the polymer blend. In some embodiments, the virgin polyolefin is visbroken. Such visbreaking of virgin polyolefin can be thermal visbreaking and/or peroxidation visbreaking. In some embodiments, such visbreaking conditions for a virgin polyolefin consist of thermal visbreaking at a temperature above the melting point of the polyolefin, greater than or equal to 300° C., or in the range of from 320° C. to 400° C., in the absence of or substantially in the absence of oxygen.

In some embodiments, the blends of processed polyolefin recyclate and a polyolefin blend component, in combination with or independently of the blend ratios in the preceding paragraph, comprise a bimodal polymer, wherein the processed polyolefin recyclate product has a weight average molecular weight (“M_(w3)”), the polyolefin blend component has a weight average molecular weight (“M_(w4)”); and M_(w3)/M_(w4) is either less than or equal to 0.9,0.8, 0.7, 0.6, or 0.5, or alternatively is greater than or equal to 1.1, 1.25, 1.5, 1.75, or 2.0.

Bimodal blends

Polyolefins with an outstanding combination of properties are so-called bimodal or multimodal polyolefins. These polyolefins are composed of two or more components having different compositions. The components of a multimodal polyolefin can differ with respect to the molecular weight and/or with respect to the comonomer composition. Multimodal polyolefin compositions are frequently prepared in a combination of two or more polymerization zones operated at different polymerization conditions. The two or more polymerization zones are usually arranged in a series of two or more polymerization reactors.

Multimodal polyolefins can be used in a wide range of applications. However, different applications need a different combination of polymer properties. Consequently, multimodal polyolefins designed to be used in different applications usually contain different components which vary with respect to molecular weight and comonomer composition and they usually contain different components in different amounts. Moreover, employing components having a narrow molecular weight distribution gives less overlap of the different components and accordingly allows a more precise tailoring of target polyolefin compositions.

Compression molding

Compression molding is a fast-running plastics conversion process for caps and closures providing an efficient processing in terms of short cycle times and low energy consumption. This results in superior performance in terms of throughput and dimensional consistency of final items. With a lower conversion temperature, material is less prone to degradation.

Polyolefins useful in injection molding processes are typically also useful in compression molding processes, including, but not limited to, production of caps and closures. In some embodiments, polyolefins for use in compression molding have pronounced shear thinning and an over proportional lower flow resistance. Such characteristics help maintain high throughput and superior characteristics on the final item produced, such as, but not limited to ESCR.

Die swell is a common phenomenon in polyolefin extrusion processes in which a melted stream of polymeric material is forced through a die. Relevant processes include, but not limited to, compression molding, injection molding, and blow molding. Die swell is a phenomenon directly related to entropy and the relaxation of the polymer within the flow stream. A polymer melt flow stream has a constant rate before entering the die, and the polymer chains within the stream occupy a roughly spherical conformation, maximizing entropy. Extrusion through the die causes an increase in polymer flow rate due in part to the reduced cross-sectional area in the die. Polymer chains in the polymer melt flowing through the die start to lose their spherical shape due to the increased flow rate. The polymer chains become more elongated and physical entanglement among polymer chains is reduced to an extent dependent upon the length of time the polymer is in the die. When the polymer stream leaves the die, the remaining physical entanglements cause polymer chains in the die stream to regain a portion of their former shape and spherical volume, in order to return to the roughly spherical conformation that maximizes entropy.

Since polymer chain disentanglement is a kinetic process, a longer die and/or lower flow rate provide more time for disentanglement. Commercial motivations place both a lower limit on polymer flow rate through the die and an upper limit on the time that the polymer can stay in the die. Therefore, there is a need for polymers less prone to a high degree of polymer chain entanglement.

One challenge with using polymer recyclate in compression molding caps or closures is excessive die swell. The die swell causes problems between the extrudate slicing step and transfer into the mold. The polymer swells into a “mushroom” top that is challenging to transfer. This swell is a material property inherent to polymer recyclate streams, particularly those with low I₂ and/or I₂₁.

Die swell is related to the elasticity of the polymer due to the possibility of the polymer system to contract and expand. When a system of random coils of entangled polymer chains enters the capillary die under melt conditions, it undergoes a contraction which, after partially relaxing in the capillary, is partially recovered at the outlet, when no longer restrained by the capillary. Swelling upon discharge from the capillary can be very strong for polyolefins, such as, but not limited to, polyethylene and/or polypropylene. The effect of swelling is critical in some polymer processes, such as, but not limited to compression molding. Too much swell can cause processing problems and defects in molded products. ISO 11443 specifies a method for the measurement of die swell through the accessories of capillary rheometers.

Since polymer chain disentanglement is a kinetic process, a longer die and/or lower flow rate provide more time for disentanglement. Commercial motivations place both a lower limit on polymer flow rate through the die and an upper limit on the time that the polymer can stay in the die. Therefore, there is a need for polymers less prone to a high degree of polymer chain entanglement.

Typically, the die swell can also be decreased by using a polymer less susceptible to such chain entanglement such as, but not limited to, polymers having shorter average chain lengths, resulting in a higher I₂ and/or I_(21.) Polymer recyclate inherently contains a significant amount of long-chain polymer, thus decreasing the I₂ and/or I₂₁ of the polymer recyclate. Dry blending and/or compounding a high I₂ and/or I₂₁ virgin polymer with polymer recyclate, which low flow polyethylene is one way to increase the overall I₂ and/or I₂₁ of the blend. However, this approach offers limited improvement to the overall die swell due to the continued presence of long molecular weight chains in the polymer recyclate component of the blend.

Polymer recyclate that has been visbroken can produce a processed polymer recyclate having a I₂ and/or I₂₁ high enough to reduce die swell during compression molding to an acceptable level. Such processed polymer recyclate can be used in compression molding operation alone or in combination with one or more virgin polymers and/or one or more other processed polymer recyclates.

Visbreaking can be accomplished by thermal visbreaking, peroxide visbreaking, or a combination thereof. a polyethylene, used neat or as part of a blend with virgin polyethylene, is a potential solution. Controlled visbreaking would target the long molecular weight chains and lower die swell, improving the processability in compression molding for caps and closures.

In some embodiments, the processed polyolefin recyclate useful in compression molding has a die swell (as measured by ASTM D3835 or ISO 11443) of less than or equal to 150%, less than or equal to 140%, less than or equal to 130%, less than or equal to 120%, less than or equal to 110%, or less than or equal to 100%.

In some embodiments, the processed polyolefin recyclate useful in compression molding has a die swell (as measured by ASTM D3835 or ISO 11443) of less than or equal to 200%, less than or equal to 190%, or less than or equal to 180%.

Certain Embodiments

In some embodiments, a method for processing high density polyethylene (“HDPE”) recyclate and/or medium density polyethylene (“MDPE”) recyclate comprises providing a polyolefin recyclate feedstock, adding the polyolefin recyclate to a first extruder to produce a first polyolefin recyclate melt, and subjecting the first polyolefin recyclate melt to visbreaking conditions to produce a second polyolefin recyclate melt. The polyolefin recyclate feedstock has: a first density in the range of from 0.900 g/cm³ to 0.970 g/cm³; a first melt index (2.16 kg, 190° C.) less than or equal to 5.0 g/10 min.; a first molecular weight distribution (M_(w)/M_(n)) greater than 6.0, greater than 8.0, or greater than 10, and/or less than 25, less than 20, or less than 15; a first weight average molecular weight (“M_(w1)”) greater than or equal to 85,000 daltons, greater than or equal to 100,000 daltons, greater than or equal to 150,000 daltons, greater than or equal to 200,000 daltons, or greater than or equal to 250,000 daltons, and/or less than or equal to 600,000 daltons, less than or equal to 500,000 daltons, less than or equal to 400,000 daltons, or less than or equal to 300,000 daltons; and a first melt elasticity (“ER”) greater than or equal to 0.5.

The second polyolefin recyclate melt has: a second density, wherein the ratio of the second density to the first density is greater than or equal to 1.0; a second melt index, wherein the ratio of the second melt index to the first melt index is greater than or equal to 5.0; a second molecular weight distribution, wherein the ratio of second molecular weight distribution to the first molecular weight distribution is less than or equal to 0.99, less than or equal to 0.95, or less than or equal to 0.80; a second weight average molecular weight (“M_(w2)”), wherein M_(w2)/M_(w1) is is less than or equal to 0.99, less than or equal to 0.95, less than or equal to 0.80, or less than or equal to 0.70; and a second melt elasticity, wherein the ratio of the second melt elasticity to the first melt elasticity is less than or equal to 0.90, less than or equal to 0.70, or less than or equal to 0.50.

In further embodiments, the method is additionally characterized by one or more of the following:

-   -   a) the polyolefin recyclate feedstock comprises post-consumer         recycled waste, post-industrial recycled waste, or a combination         thereof;     -   b) the visbreaking conditions consist of thermal visbreaking,         which in some instances is performed at a temperature greater         than or equal to 300° C., or at a temperature in the range of         from 320° C. to 400° C.;     -   c) the first HDPE polyolefin recyclate melt is further subjected         to devolatilization conditions to produce the second polyolefin         recyclate melt, wherein the polyolefin recyclate feedstock has a         first volatile organic compound content, the first HDPE         polyolefin recyclate melt has a second volatile organic compound         content, and the ratio of the second volatile organic compound         content to the first volatile organic compound content is less         than or equal to 0.9, and in some instances, the         devolatilization conditions further comprise:         -   i) injection and withdrawal of a scavenging gas, and in some             instances the scavenging gas comprises nitrogen,             carbon-dioxide, water, or combinations thereof;         -   ii) vent conditions, vacuum conditions, or a combination             thereof;     -   d) the second polyolefin recyclate melt is passed through a melt         filter;     -   e) an antioxidant agent is added to the first extruder; and     -   f) the polyolefin recyclate feedstock has a first high load melt         index (21.6 kg, 190° C.), the second polyolefin recyclate melt         has a second high load melt index, and the ratio of the second         high load melt index to the first high load melt index is         greater than or equal to 2.0, greater than or equal to 3.0,         greater than or equal to 4.0, or greater than or equal to 5.0;     -   g) the polyolefin recyclate feedstock has a first melt index         ratio (I₂₁/I₂), the second polyolefin recyclate melt has a         second melt index ratio, and the ratio of the second melt index         ratio to the first melt index ratio is less than or equal to         0.90, less than or equal to 0.85, less than or equal to 0.80, or         less than or equal to 0.75;     -   h) an overall polydispersity measure (“PDR”), the second         polyolefin recyclate melt has a second PDR, and the ratio of the         second PDR to the first PDR is less than or equal to 0.90, less         than or equal to 0.80, less than or equal to 0.70, or less than         or equal to 0.50;     -   i) the polyolefin recyclate feedstock has a first complex         complex viscosity ratio (η*_(0.1)/η*₁₀₀), the second polyolefin         recyclate melt has a complex viscosity ratio, and the ratio of         the second complex viscosity ratio to the first complex         viscosity ratio is less than or equal to 0.70, less than or         equal to 0.60, less than or equal to 0.50, or less than or equal         to 0.40; and     -   j) the polyolefin recyclate feedstock has a first intrinsic         viscosity [η], the second polyolefin recyclate melt has a         intrinsic viscosity, and the ratio of the second intrinsic         viscosity to the first intrinsic viscosity is less than or equal         to 0.70, less than or equal to 0.60, less than or equal to 0.50,         or less than or equal to 0.40.

In some embodiments, the foregoing method further comprises forming a polyolefin recyclate product by withdrawal of the second polyolefin recyclate melt from the first extruder for further processing or pelletizing of the second polyolefin recyclate melt.

In further embodiments of the foregoing method, the polyolefin recyclate product and a first polyolefin blend component are added to a second extruder, and compounding conditions are effected in the second extruder to form a polyolefin product comprising the melt-blended mixture of the processed polyolefin recyclate product and the first polyolefin blend component. In some embodiments, such compounding condition include a temperature less than or equal to 300° C. In some embodiments, the first polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof. In yet further embodiments: the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin polyolefin, a virgin MDPE, a virgin polypropylene, or a combination thereof; the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a polyolefin recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof and the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed HDPE recyclate, a processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof. In some embodiments, the first polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof.

In further embodiments of the foregoing method, the polyolefin recyclate product: is added in an amount in the range of from 5 wt. % to 90 wt. %, or from 20 wt. % to 60 wt. %, based on the combined weight of the polyolefin recyclate product and the first polyolefin blend component; and/or the polyolefin recyclate product has third weight average molecular weight (“M_(w3)”), the first polyolefin blend component has a fourth weight average molecular weight (“M_(w4)”), and

the M_(w3)/M_(w3) is either less than or equal to 0.8 or greater than or equal to 1.25.

In further embodiments of the foregoing method, the first polyolefin blend component is a first virgin polyolefin comprising a polymer product prepared in a first polymerization apparatus, wherein in some instances, the polymer product was subjected to a visbreaking process after polymerization, and in some embodiments, the visbreaking process comprises thermal visbreaking, peroxide visbreaking, or a combination thereof.

In further embodiments of the foregoing method, the first polyolefin blend component comprises a polyolefin powder prepared in a first polymerization apparatus.

In further embodiments of the foregoing method, an antioxidant agent is added to the second extruder.

In further embodiments of the foregoing method, the method further comprises: adding a second polyolefin blend component to a third extruder; effecting melt conditions in the third extruder to produce a second polyolefin blend component melt; and withdrawing the second polyolefin blend component melt as the first polyolefin blend component.

In further embodiments of the foregoing method, the second polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof.

In further embodiments of the foregoing method, the second polyolefin blend component is subjected to a visbreaking process after polymerization, wherein in some instances, the visbreaking process consists of thermal visbreaking.

In further embodiments of the foregoing method, the second polyolefin blend component comprises polyethylene powder prepared in a second polymerization apparatus and/or polyethylene pellets.

In further embodiments of the foregoing method, the first and/or second polymerization apparatus each comprise two more polymerization reactors and/or two or more polymerization zones within a polymerization reactor.

In further embodiments of the foregoing method, the first and/or second polymerization apparatuses each comprise two or more gas phase fluidized-bed reactors in series, two or more slurry phase reactors in series, or a gas phase fluidized-bed reactor in series with a multizone circulation reactor.

In further embodiments of the foregoing method, an antioxidant agent is added to the third extruder.

In some embodiments, a composition comprise a polymer blend of a first polymer and a second polymer. The first polymer is a first processed polyolefin recyclate and is present in an amount in the range of from 5 wt. % to 90 wt. %. The second polymer is a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof, and is present in an amount in the range of from 10 wt. % to 95 wt. %. All weight percentages are based on the combined weight of the first and second polymers.

In further embodiments of the foregoing composition: the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof; the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof; and the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a second processed HDPE recyclate, a second processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof.

In further embodiments of the foregoing composition, processed means subjected to thermal visbreaking or subjected to thermal visbreaking and devolatilization. In some embodiments, a blend comprises a visbroken polyolefin, having a first I₂ and a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof, having a second I₂, wherein:

${\log\left( \left( I_{2} \right)_{blend} \right)} = {\sum\limits_{i = 1}^{n}\left( {w_{i} \times {\log\left( \left( I_{2} \right)_{i} \right)}} \right)}$

(I₂)_(blend) is the target melt index of the final blend product;

n is the number of components in the blend; and

i is the i-th component of an n-component blend.

The following examples illustrate the invention; however, those skilled in the art will recognize numerous variations within the spirit of the invention and scope of the claims. To facilitate a better understanding of the present invention, the following examples of preferred embodiments are given. In no way should the following examples be read to limit, or to define, the scope of the invention.

EXAMPLES

The following examples are included to demonstrate preferred embodiments of the invention. It should be appreciated by those of skill in the art that the techniques disclosed in the examples which follow represent techniques discovered by the inventor to function well in the practice of the invention, and thus can be considered to constitute preferred modes for its practice. However, those of skill in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the spirit and scope of the invention.

The following examples use commercial HDPE compositions having a low melt index as proxies for HDPE recyclate feedstocks. After processing, as described herein, the visbroken low melt index HDPEs, either alone or in blends with other components, are compared to higher melt index virgin HDPEs.

Test Methods

Densities are determined in accordance with ASTM D-4703 and ASTM D-1505/ISO-1183.

Die swell is determined herein by an internally developed test using a Goetfert Rheograph 25 capillary rheometer. The polymer melt is extruded from the die at a temperature of 190° C. at a shear rate of 525 s-1. The die swell of the extrudate is measured via a laser positioned at 78 mm below the bottom of the die. The die has an orifice diameter of 1 mm with an L/D of 0.25 and a 90° entry angle. The extrudate strand is cut before measurement at a position of 120 mm below the bottom of the die.

High load melt index (“I₂₁”) was determined by ASTM D-1238-F (190° C./21.6 kg).

Shear rheological measurements are performed in accord with ASTM 4440-95a, which characterize dynamic viscoelastic properties (storage modulus, G′, loss modulus, G″ and complex viscosity, η^(*), as a function of oscillation frequency, ω). A rotational rheometer (TA Instruments) is used for the rheological measurements. A 25 mm parallel-plate fixture was utilized. Samples were compression molded in disks (˜29 mm diameter and ˜1.3 mm thickness) using a hot press at 190° C. An oscillatory frequency sweep experiment (from 398.1 rad/s to 0.0251 rad/s) was applied at 190° C. The applied strain amplitude is ˜10% and the operating gap is set at 1 mm. Nitrogen flow was applied in the sample chamber to minimize thermal oxidation during the measurement.

Melt elasticity (“ER”) is determined as discussed in R. Shroff and H. Mavridis, “New Measures of Polydispersity from Rheological Data on Polymer Melts,” J. Applied Polymer Science 57 (1995) 1605. See also U.S. Pat. Nos 7,238,754, 6,171,993 and 5,534,472 (col. 10, lines 20-30), the teachings of which are incorporated herein by reference. Thus, storage modulus (G′) and loss modulus (G″) are measured. The nine lowest frequency points are used (five points per frequency decade) and a linear equation is fitted by least-squares regression to log G′ versus log G″. ER is then calculated from:

ER=(1.781×10⁻³)×G′

at a value of G″=5,000 dyn/cm². The same procedure and equation for the ER calculation was used for both linear and long-chain-branched polyolefins.

PDR, or “Overall Polydispersity Measure” is determined as discussed in R. Shroff and H. Mavridis, “New Measures of Polydispersity from Rheological Data on Polymer Melts,” J. Applied Polymer Science 57 (1995) 1605, equation 27 on page 1619, with G*_(ref,1)=1.95*10⁴ dyn/cm² and log₁₀(G*_(ref,3)/G*_(ref,1))=2. The same procedure and equation for the PDR calculation was used for both linear and long-chain-branched polyolefins.

The ratio η*_(0.1)/η*₁₀₀ of complex viscosities, η*_(0.1), at a frequency of 0.1 rad/sec and η*₁₀₀, at a frequency of 100 rad/sec, is used as an additional measure of shear sensitivity and thus rheological breadth, or polydispersity, of the polymer melt.

Melt index (“I₂”) was determined by ASTM D-1238-E (190° C./2.16 kg).

Melt flow rate (“MFR”) was determined by ASTM D-1238-L (230° C./2.16 kg).

Molecular weight distribution (“MWD”) as well as the molecular weight averages (number-average molecular weight, M_(n) weight-average molecular weight, M_(w), and z-average molecular weight, M_(z)) are determined using a high temperature Polymer Char gel permeation chromatography (“GPC”), also referred to as size exclusion chromatography (“SEC”), equipped with a filter-based infrared detector, IR5, a four-capillary differential bridge viscometer, and a Wyatt 18-angle light scattering detector. M_(n), M_(w), M_(z), MWD, and short chain branching (SCB) profiles are reported using the IR detector, whereas long chain branch parameter, g′, is determined using the combination of viscometer and IR detector at 145° C. Three Agilent PLgel Olexis GPC columns are used at 145° C. for the polymer fractionation based on the hydrodynamic size in 1,2,4-trichlorobenzene (TCB) with 300 ppm antioxidant butylated hydroxytoluene (BHT) as the mobile phase. 16 mg polymer is weighted in a 10 mL vial and sealed for the GPC measurement. The dissolution process is obtained automatically (in 8 ml TCB) at 160° C. for a period of 1 hour with continuous shaking in an Agilent autosampler. 20 μL Heptane was also injected in the vial during the dissolution process as the flow marker. After the dissolution process, 200 μL solution was injected in the GPC column. The GPC columns are calibrated based on twelve monodispersed polystyrene (PS) standards (provided by PSS) ranging from 578 g/mole to 3,510,000 g/mole. The comonomer compositions (or SCB profiles) are reported based on different calibration profiles obtained using a series of relatively narrow polyethylene (polyethylene with 1-hexene and 1-octene comonomer were provided by Polymer Char, and polyethylene with 1-butene were synthesized internally) with known values of CH₃/1000 total carbon, determined by an established solution NMR technique. GPC one software was used to analyze the data. The long chain branch parameter, g′, is determined by the equation:

g′=[η]/[η]_(lin)

where, [η] is the average intrinsic viscosity of the polymer that is derived by summation of the slices over the GPC profiles as follows:

$\lbrack\eta\rbrack = \frac{\sum{c_{i}\lbrack\eta\rbrack}_{i}}{\sum c_{i}}$

where c_(i) is the concentration of a particular slice obtained from IR detector, and [η]_(i) is the intrinsic viscosity of the slice measured from the viscometer detector. [η]_(lin) is obtained from the IR detector using Mark-Houwink equation ([η]_(lin)=ΣKM_(i) ^(α)) for a linear high density polyethylene, where M_(i) is the viscosity-average molecular weight for a reference linear polyethylene, K and α are Mark-Houwink constants for a linear polymer, which are K=0.000374, α=0.7265 for a linear polyethylene and K=0.00041, α=0.6570 for a linear polypropylene.

Volatile Organic Compounds (“VOC”) is measured by pyrolysis-gas chromatography/mass spectrometry (“P-GC/MS”) in parts per billion (ppb), parts per million (ppm), or and micrograms per cubic meter (μg/m³).

Zero-shear viscosity, η₀, is determined using the Sabia equation fit of dynamic complex viscosity versus radian frequency, as described in of Shroff & Mavridis, (1999) “A Long Chain Branching Index for Essentially Linear Polyethylenes”, Macromolecules, 32, 8454-8464 (with focus on Appendix B), the disclosure of which is fully incorporated by reference herein in its entirety.

LCBI is determined using equation 13:

$\begin{matrix} {{LCBI} = {{\frac{\eta_{0}^{0.17}}{\eta}\frac{1}{4.8}} - 1}} & (13) \end{matrix}$

Equation 13 and its application are described in of Shroff & Mavridis, (1999) “A Long Chain Branching Index for Essentially Linear Polyethylenes”, Macromolecules, 32, 8454-8464, the disclosure of which is fully incorporated by reference herein in its entirety.

Long Chain Branching frequency, characterized by the ratio of Long Chain Branches per million carbon atoms, or LCB/10⁶ C, was determined by the method of Janzen & Colby (J. Janzen and R. H. Colby, “Diagnosing long-chain branching in polyethylenes”, Journal of Molecular Structure, Vol 485-486, 10 Aug. 1999, Pages 569-583), using eqs. (2-3) and the constants of Table 2 in the above reference. Specifically, the zero-shear viscosity at 190° C., η*₀, is determined by extrapolation of the complex viscosity data via the Sabia equation, as described separately. The weight-average-molecular weight, Mw, is determined via GPC. With these two parameters and the methodology of Janzen & Colby, the Long Chain Branching frequency, LCB/10⁶ C, can be determined numerically such that all 3 parameters (η₀, M_(w) and LCB/10⁶ C) satisfy eqs. (2-3) in the above reference. The Janzen & Colby methodology predicts that the ratio, η₀/η_(0,linear) of the zero-shear viscosity of the material, over the zero-shear viscosity of a perfectly linear polymer (LCB/10⁶ C=0) of the same average molecular weight, exhibits a maximum at a certain value of LCB/10⁶ C and therefore for every value of η₀/η_(0,linear), there exist two levels, or values, of LCB/10⁶ C that such ratio is possible. For the purposes of the present calculations, the lowermost value of LCB/10⁶ C was always selected at the given ratio of η₀/η_(0,linear).

Raw Materials

Raw materials used herein are shown in Table 1, below.

TABLE 1 Polymer MFR Density Composition Use in Examples Label (g/10 min) (g/cc) LyondellBasell ™ Proxy for LLDPE P1 2.1**  0.921 HF1820 * recyclate feedstock Petrothene ™ Proxy for LDPE P2 0.62** 0.923 NA963083 LDPE * recyclate feedstock Petrothene ™ Proxy for HDPE P3 0.8**  0.960 LM600700 * homopolymer recyclate Pro-fax SR257M ™ * Proxy for PP random P4 2.0*** 0.90 copolymer recyclate Pro-fax SC204 ™ * Proxy for PP impact P5 4.0*** 0.90 copolymer recyclate * Available from LyondellBasell Industries NV **190° C./2.16 kg ***230° C./2.16 kg

Examples 1-9

Examples 1-9 in TABLE 2 show the results of visbreaking a LLDPE, a LDPE, and blends thereof. P1 is believed to fairly represent an LLDPE recyclate feedstock. P2 is believed to fairly represent a LDPE recyclate feedstock. Examples 2-8 were prepared by visbreaking portions of P1, P2, and blends thereof. Visbreaking was performed by feeding P1, P2, and blends thereof into a Werner and Pfleiderer ZSK40 twin screw extruder at a feed rate of 50 pounds per hour, a screw speed of 600 rpm and with a target temperature profile of 200/250/325/325/325/325/325/325/325° C. (from feed inlet to die). Examples 3-7 show changes to I₂, density, HLMI, HLMI/MI, ER, PDR, η₀, η*_(0.1), η*₁₀₀, η*_(0.1)/η*₁₀₀, M_(w), M_(z), M_(w)/M_(n), M_(z)/M_(w), IV, g′, and LCBI produced by visbreaking blends of P1 and P2.

TABLE 2 Example Parameter Units 1 2 3 4 P1 wt % 100 100 85 70 P2 wt % 0 0 15 30 Visbroken — no yes yes yes I₂ g/10 min 2.1 15.0 16.7 12.5 Density — 0.921 0.924 HLMI g/cc 60.1 HLMI/MI g/10 min 29 ER — 0.63 0.29 0.50 0.78 PDR — 3.5 2.2 2.8 4.1 η₀ poise 4.67E+04 5.48E+03 5.57E+03 8.48E+03 η*_(0.1) poise 4.19E+04 5.46E+03 5.46E+03 7.99E+03 η*₁₀₀ poise 1.10E+04 3.34E+03 2.88E+03 3.12E+03 η*_(0.1)/η*₁₀₀ — 3.8 1.6 1.9 2.6 Mw daltons 110,400 63,300 63,900 67,900 Mz daltons 338,400 155,000 166,800 192,100 Mw/Mn — 5.3 4.2 4.4 4.8 Mz/Mw — 3.1 2.4 2.6 2.8 IV — 1.44 0.93 0.89 0.87 g′ — 0.95 0.89 0.85 0.81 LCBI — −0.01 0.05 0.10 0.21 g′_calculated — — 0.89 0.84 0.79 (visbroken) g′_calculated — 0.95 — 0.89 0.84 (original) I₂ blend g/10 min 2.09 — 1.74 1.45 calculated −> original I₂ blend g/10 min — 15.0 12.6 10.6 calculated −> visbroken Example Parameter Units 5 6 7 8 9 P1 wt % 50 30 15 0 0 P2 wt % 50 70 85 100 100 Visbroken — yes yes yes yes no I₂ g/10 min 10.1 7.6 6.0 4.8 0.62 Density — 0.923 HLMI g/cc 50 HLMI/MI g/10 min 81 ER — 1.08 1.23 1.37 1.53 2.37 PDR — 6.6 10.7 16.3 26 77 η₀ poise 1.23E+04 1.91E+04 2.56E+04 3.59E+04 4.26E+05 η*_(0.1) poise 1.15E+04 1.74E+04 2.25E+04 2.98E+04 1.78E+05 η*₁₀₀ poise 3.21E+03 3.41E+03 3.41E+03 3.42E+03 6.39E+03 η*_(0.1)/η*₁₀₀ — 3.6 5.1 6.6 9 28 Mw daltons 74,500 82,700 87,900 94,500 129,900 Mz daltons 226,500 266,100 289,900 318,100 396,500 Mw/Mn — 5.4 6.2 6.6 7.3 7.8 Mz/Mw — 3.0 3.2 3.3 3.4 3.1 IV — 0.85 0.85 0.83 0.83 1.03 g′ — 0.74 0.69 0.65 0.62 0.61 LCBI — 0.32 0.43 0.54 0.64 1.06 g′_calculated — 0.74 0.69 0.66 0.62 0.00 (visbroken) g′_calculated — 0.77 0.70 0.66 — 0.61 (original) I₂ blend g/10 min 1.14 0.89 0.74 — 0.62 calculated −> original I₂ blend g/10 min 8.4 6.7 5.6 4.8 — calculated −> visbroken

Dynamic oscillatory data generated based on analysis of Examples 1-9 are shown in TABLE 3 below. The data in TABLE 3 show that complex viscosity decreases as frequency increases for Examples 1-9. TABLE 3 further shows that visbroken blends of LLDPE and LDPE in Examples 2-8 have a lower complex viscosity (η*)for all tested values of frequency.

TABLE 3 Example 1 2 3 4 Freq. η* Freq. η* Freq. η* Freq. η* rad/sec poise rad/sec Poise rad/sec poise rad/sec poise 3.98E+02 5.58E+03 3.98E+02 2.31E+03 3.98E+02 1.93E+03 3.98E+02 1.99E+03 2.51E+02 7.15E+03 2.51E+02 2.68E+03 2.51E+02 2.25E+03 2.51E+02 2.34E+03 1.58E+02 8.93E+03 1.58E+02 3.00E+03 1.58E+02 2.56E+03 1.58E+02 2.71E+03 1.00E+02 1.10E+04 1.00E+02 3.34E+03 1.00E+02 2.88E+03 1.00E+02 3.12E+03 6.31E+01 1.33E+04 6.31E+01 3.69E+03 6.31E+01 3.20E+03 6.31E+01 3.58E+03 3.98E+01 1.58E+04 3.98E+01 4.02E+03 3.98E+01 3.53E+03 3.98E+01 4.08E+03 2.51E+01 1.85E+04 2.51E+01 4.29E+03 2.51E+01 3.83E+03 2.51E+01 4.57E+03 1.58E+01 2.14E+04 1.58E+01 4.53E+03 1.58E+01 4.11E+03 1.58E+01 5.07E+03 1.00E+01 2.42E+04 1.00E+01 4.72E+03 1.00E+01 4.35E+03 1.00E+01 5.56E+03 6.31E+00 2.70E+04 6.31E+00 4.86E+03 6.31E+00 4.58E+03 6.31E+00 6.01E+03 3.98E+00 2.96E+04 3.98E+00 4.99E+03 3.98E+00 4.77E+03 3.98E+00 6.46E+03 2.51E+00 3.18E+04 2.51E+00 5.08E+03 2.51E+00 4.93E+03 2.51E+00 6.86E+03 1.58E+00 3.40E+04 1.58E+00 5.15E+03 1.58E+00 5.06E+03 1.58E+00 7.20E+03 1.00E+00 3.59E+04 1.00E+00 5.19E+03 1.00E+00 5.15E+03 1.00E+00 7.48E+03 6.31E−01 3.76E+04 6.31E−01 5.23E+03 6.31E−01 5.21E+03 6.31E−01 7.69E+03 3.98E−01 3.90E+04 3.98E−01 5.26E+03 3.98E−01 5.25E+03 3.98E−01 7.83E+03 2.51E−01 4.02E+04 2.51E−01 5.29E+03 2.51E−01 5.26E+03 2.51E−01 7.92E+03 1.58E−01 4.11E+04 — — 1.58E−01 5.28E+03 1.58E−01 7.97E+03 1.00E−01 4.19E+04 — — — — 1.00E−01 7.99E+03 6.31E−02 4.25E+04 — — — — 6.31E−02 7.99E+03 3.98E−02 4.30E+04 — — — — — — 2.51E−02 4.35E+04 — — — — — — 5 6 7 8 9 Freq. η* Freq. η* Freq. η* Freq. η* Freq. η* rad/sec poise rad/sec poise rad/sec poise rad/sec poise rad/sec poise 3.98E+02 1.85E+03 3.98E+02 1.81E+03 3.98E+02 1.70E+03 3.98E+02 1.61E+03 3.98E+02 2.62E+03 2.51E+02 2.26E+03 2.51E+02 2.27E+03 2.51E+02 2.18E+03 2.51E+02 2.10E+03 2.51E+02 3.56E+03 1.58E+02 2.71E+03 1.58E+02 2.80E+03 1.58E+02 2.74E+03 1.58E+02 2.69E+03 1.58E+02 4.77E+03 1.00E+02 3.21E+03 1.00E+02 3.41E+03 1.00E+02 3.41E+03 1.00E+02 3.42E+03 1.00E+02 6.39E+03 6.31E+01 3.78E+03 6.31E+01 4.13E+03 6.31E+01 4.22E+03 6.31E+01 4.32E+03 6.31E+01 8.47E+03 3.98E+01 4.42E+03 3.98E+01 4.98E+03 3.98E+01 5.20E+03 3.98E+01 5.41E+03 3.98E+01 1.12E+04 2.51E+01 5.11E+03 2.51E+01 5.92E+03 2.51E+01 6.32E+03 2.51E+01 6.74E+03 2.51E+01 1.46E+04 1.58E+01 5.84E+03 1.58E+01 6.98E+03 1.58E+01 7.59E+03 1.58E+01 8.26E+03 1.58E+01 1.90E+04 1.00E+01 6.61E+03 1.00E+01 8.12E+03 1.00E+01 9.01E+03 1.00E+01 1.00E+04 1.00E+01 2.45E+04 6.31E+00 7.37E+03 6.31E+00 9.36E+03 6.31E+00 1.06E+04 6.31E+00 1.20E+04 6.31E+00 3.15E+04 3.98E+00 8.16E+03 3.98E+00 1.06E+04 3.98E+00 1.22E+04 3.98E+00 1.41E+04 3.98E+00 3.98E+04 2.51E+00 8.91E+03 2.51E+00 1.19E+04 2.51E+00 1.39E+04 2.51E+00 1.63E+04 2.51E+00 5.00E+04 1.58E+00 9.60E+03 1.58E+00 1.31E+04 1.58E+00 1.57E+04 1.58E+00 1.87E+04 1.58E+00 6.23E+04 1.00E+00 1.02E+04 1.00E+00 1.43E+04 1.00E+00 1.73E+04 1.00E+00 2.11E+04 1.00E+00 7.67E+04 6.31E−01 1.07E+04 6.31E−01 1.53E+04 6.31E−01 1.88E+04 6.31E−01 2.34E+04 6.31E−01 9.34E+04 3.98E−01 1.10E+04 3.98E−01 1.61E+04 3.98E−01 2.01E+04 3.98E−01 2.54E+04 3.98E−01 1.12E+05 2.51E−01 1.13E+04 2.51E−01 1.67E+04 2.51E−01 2.12E+04 2.51E−01 2.72E+04 2.51E−01 1.33E+05 1.58E−01 1.14E+04 1.58E−01 1.71E+04 1.58E−01 2.20E+04 1.58E−01 2.87E+04 1.58E−01 1.55E+05 1.00E−01 1.15E+04 1.00E−01 1.74E+04 1.00E−01 2.25E+04 1.00E−01 2.98E+04 1.00E−01 1.78E+05 6.31E−02 1.16E+04 6.31E−02 1.75E+04 6.31E−02 2.28E+04 6.31E−02 3.05E+04 6.31E−02 2.00E+05 3.98E−02 1.16E+04 3.98E−02 1.76E+04 3.98E−02 2.30E+04 3.98E−02 3.10E+04 3.98E−02 2.21E+05 2.51E−02 1.16E+04 2.51E−02 1.76E+04 2.51E−02 2.31E+04 2.51E−02 3.14E+04 2.51E−02 2.39E+05

Examples 10-17

Examples 10-17 in TABLE 4 show the results of visbreaking a HDPE, a PP, and blends thereof. P3 is believed to fairly represent an HDPE recyclate feedstock. P4 is believed to fairly represent a PP recyclate feedstock. Examples 11-15 were prepared by visbreaking portions of P3, P4, and blends thereof. Visbreaking was performed by feeding P3, P4, and blends thereof into a Werner and Pfleiderer ZSK40 twin screw extruder at a feed rate of 50 pounds per hour, a screw speed of 600 rpm and with a target temperature profile of 200/250/325/325/325/325/325/325/325° C. (from feed inlet to die). Examples 12-14 show changes to I2, MFR, ER, PDR, η0@ 200° C., η0@ 190° C., η*0.1, η*100, η*0.1/η*100, Mw, Mz, Mw/Mn, Mz/Mw, IV, g′, and LCBI produced by visbreaking blends of P3 and P4.

TABLE 4 Example Parameter Units 10 11 12 13 P3 wt % 100 100 99 95 P4 wt % 0 0 1 5 Visbroken — no yes yes yes I₂ g/10 min 0.764 8 7 6 MFR g/10 min 1.3 16 13 12 ER — 3.63 1.01 1.12 1.24 PDR — 18.9 5.9 6.9 7.2 η₀@ 200° C. poise 1.33E+04 1.81E+04 2.05E+04 η₀@ 190° C. poise 1.61E+06 1.54E+04 2.10E+04 2.38E+04 η*_(0.l) poise 1.70E+05 1.25E+04 1.66E+04 1.83E+04 η*₁₀₀ poise 10800 3550 3940 4040 η*_(0.l) /η*₁₀₀ — 15.7 3.5 4.2 4.5 Mw daltons 130,600 59,700 63,200 66,100 Mz daltons 694,000 133,900 146,400 156,700 Mw/Mn — 7.0 3.7 3.9 4.0 Mz/Mw — 5.3 2.2 2.3 2.4 IV (Vis) dl/g 1.59 0.82 0.84 0.86 g′ — 0.98 0.82 0.81 0.80 LCBI — 0.69 0.43 0.47 0.47 Example Parameter Units 14 15 16 17 P3 wt % 90 0 0 90 P4 wt % 10 100 100 10 Visbroken — yes yes No no I₂ g/10 min 6 0.80 MFR g/10 min 12 25 2.1 1.40 ER — 1.54 0.37 1.11 4.01 PDR — 8.2 2.1 3.7 23.0 η₀@ 200° C. poise 2.42E+04 7.30E+03 1.43E+05 2.01E+06 η₀@ 190° C. poise 2.81E+04 8.47E+03 1.66E+05 2.34E+06 η*_(0.l) poise 2.01E+04 — 1.03E+05 1.49E+05 η*₁₀₀ poise 3940 2960 8680 9.17E+03 η*_(0.l) /η*₁₀₀ — 5.1 — 11.9 16.2 Mw daltons 70,500 182,300 373,800 — Mz daltons 169,500 342,800 999,300 — Mw/Mn — 4.1 4.0 5.6 — Mz/Mw — 2.4 1.9 2.7 — IV (Vis) dl/g 0.88 0.97 1.67 — g′ — 0.79 0.90 1.01 — LCBI — 0.48 0.08 0.07 —

Dynamic oscillatory data generated based on analysis of Examples 11-16 are shown in TABLE 5 below. The data in TABLE 5 show that complex viscosity decreases as frequency increases for Examples 11-16. TABLE 3 further shows that visbroken blends of HDPE and PP in Examples 12-14 have a lower complex viscosity (η^(*)) for all tested values of frequency.

TABLE 5 Example 11 12 13 Frequency η* Frequency η* Frequency η* rad/sec poise rad/sec poise rad/sec poise 3.98E+02 2.11E+03 3.98E+02 2.27E+03 3.98E+02 2.30E+03 2.51E+02 2.55E+03 2.51E+02 2.78E+03 2.51E+02 2.82E+03 1.58E+02 3.01E+03 1.58E+02 3.32E+03 1.58E+02 3.39E+03 1.00E+02 3.55E+03 1.00E+02 3.94E+03 1.00E+02 4.04E+03 6.31E+01 4.16E+03 6.31E+01 4.66E+03 6.31E+01 4.79E+03 3.98E+01 4.87E+03 3.98E+01 5.47E+03 3.98E+01 5.63E+03 2.51E+01 5.61E+03 2.51E+01 6.41E+03 2.51E+01 6.61E+03 1.58E+01 6.42E+03 1.58E+01 7.42E+03 1.58E+01 7.65E+03 1.00E+01 7.25E+03 1.00E+01 8.50E+03 1.00E+01 8.77E+03 6.31E+00 8.09E+03 6.31E+00 9.63E+03 6.31E+00 9.96E+03 3.98E+00 8.89E+03 3.98E+00 1.07E+04 3.98E+00 1.11E+04 2.51E+00 9.66E+03 2.51E+00 1.19E+04 2.51E+00 1.24E+04 1.58E+00 1.04E+04 1.58E+00 1.29E+04 1.58E+00 1.36E+04 1.00E+00 1.10E+04 1.00E+00 1.39E+04 1.00E+00 1.48E+04 6.31E−01 1.15E+04 6.31E−01 1.48E+04 6.31E−01 1.58E+04 3.98E−01 1.19E+04 3.98E−01 1.55E+04 3.98E−01 1.68E+04 2.51E−01 1.22E+04 2.51E−01 1.60E+04 2.51E−01 1.75E+04 1.58E−01 1.24E+04 1.58E−01 1.64E+04 1.58E−01 1.80E+04 1.00E−01 1.25E+04 1.00E−01 1.66E+04 1.00E−01 1.83E+04 6.31E−02 1.25E+04 6.31E−02 1.67E+04 6.31E−02 1.85E+04 3.98E−02 1.26E+04 3.98E−02 1.68E+04 3.98E−02 1.86E+04 2.51E−02 1.25E+04 2.51E−02 1.68E+04 2.51E−02 1.87E+04 Example 14 15 16 Frequency η* Frequency η* Frequency η* rad/sec poise rad/sec poise rad/sec poise 3.98E+02 2.20E+03 3.98E+02 1.69E+03 3.98E+02 3.48E+03 2.51E+02 2.72E+03 2.51E+02 2.11E+03 2.51E+02 4.82E+03 1.58E+02 3.28E+03 1.58E+02 2.50E+03 1.58E+02 6.53E+03 1.00E+02 3.94E+03 1.00E+02 2.96E+03 1.00E+02 8.68E+03 6.31E+01 4.69E+03 6.31E+01 3.48E+03 6.31E+01 1.14E+04 3.98E+01 5.55E+03 3.98E+01 4.07E+03 3.98E+01 1.48E+04 2.51E+01 6.54E+03 2.51E+01 4.67E+03 2.51E+01 1.89E+04 1.58E+01 7.59E+03 1.58E+01 5.23E+03 1.58E+01 2.39E+04 1.00E+01 8.73E+03 1.00E+01 5.73E+03 1.00E+01 2.96E+04 6.31E+00 9.94E+03 6.31E+00 6.12E+03 6.31E+00 3.61E+04 3.98E+00 1.12E+04 3.98E+00 6.43E+03 3.98E+00 4.34E+04 2.51E+00 1.24E+04 2.51E+00 6.65E+03 2.51E+00 5.10E+04 1.58E+00 1.37E+04 1.58E+00 6.80E+03 1.58E+00 5.90E+04 1.00E+00 1.50E+04 1.00E+00 6.91E+03 1.00E+00 6.70E+04 6.31E−01 1.63E+04 6.31E−01 6.97E+03 6.31E−01 7.51E+04 3.98E−01 1.76E+04 3.98E−01 7.02E+03 3.98E−01 8.27E+04 2.51E−01 1.87E+04 2.51E−01 7.05E+03 2.51E−01 9.03E+04 1.58E−01 1.95E+04 1.58E−01 7.06E+03 1.58E−01 9.73E+04 1.00E−01 2.01E+04 — — 1.00E−01 1.03E+05 6.31E−02 2.05E+04 — — 6.31E−02 1.08E+05 3.98E−02 2.07E+04 — — 3.98E−02 1.12E+05 2.51E−02 2.08E+04 — — 2.51E−02 1.15E+05

FIG. 7 a comparison of molecular weight curves generated for Examples 4 and 5. The overlaid graphs demonstrate both the reduction in molecular weight and narrowing of molecular weight distribution accomplished through visbreaking.

Examples 18-25

Examples 18-25 in TABLE 6 show the results of visbreaking a HDPE, a PP, and blends thereof. P3 is believed to fairly represent an HDPE recyclate feedstock. P5 is believed to fairly represent a PP recyclate feedstock. Examples 19-23 were prepared by visbreaking portions of P3, P5, and blends thereof. Visbreaking was performed by feeding P3, P5, and blends thereof into a Werner and Pfleiderer ZSK40 twin screw extruder at a feed rate of 50 pounds per hour, a screw speed of 600 rpm and with a target temperature profile of 200/250/325/325/325/325/325/325/325° C. (from feed inlet to die). Examples 20-22 show changes to I₂, MFR, ER, PDR, η0@200° C, η0@190° C., η*_(0.1), η*₁₀₀, η*_(0.1)/η*₁₀₀, M_(w), M_(z), M_(w)/M_(n), M_(z)/M_(w), IV, g′, and LCBI produced by visbreaking blends of P3 and P4.

TABLE 6 Example Parameter Units 18 19 20 21 P3 wt % 100 100 99 95 P4 wt % 0 0 1 5 Visbroken — no yes yes yes I₂ g/10 min 0.764 8 8 6 MFR g/10 min 1.3 16 14 12 ER — 3.63 1.01 1.1 1.3 PDR — 18.9 5.88 6.567 7.568 η₀@ 200° C. poise 1.33E+04 1.52E+04 2.25E+04 η₀@ 190° C. poise 1.61E+06 1.54E+04 1.76E+04 2.61E+04 η*_(0.l) poise 1.25E+04 1.41E+04 1.98E+04 η*₁₀₀ poise 3550 3610 4120 η*_(0.l) /η*₁₀₀ — 3.5 3.9 4.8 Mw daltons 130,600 59,700 61,600 67,000 Mz daltons 694,000 133,900 141,000 158,800 Mw/Mn — 7.0 3.7 3.9 4.0 Mz/Mw — 5.3 2.2 2.3 2.4 IV (Vis) dl/g 1.59 0.82 0.84 0.87 g′ — 0.98 0.82 0.82 0.81 LCBI — 0.69 0.43 0.43 0.48 Example Parameter Units 22 23 24 25 P3 wt % 90 0 0 90 P4 wt % 10 100 100 10 Visbroken — yes yes No no I₂ g/10 min 5 0.84 MFR g/10 min 10 19 4.1 1.46 ER — 1.7 0.95 1.25 3.97 PDR — 8.891 2.89E+00 4.01E+00 24.9 η₀@ 200° C. poise 3.63E+04 1.32E+04 7.84E+04 2.65E+06 η₀@ 190° C. poise 4.21E+04 1.53E+04 9.10E+04 3.07E+06 η*_(0.l) poise 2.77E+04 1.23E+04 5.99E+04 1.49E+05 η*₁₀₀ poise 4530 3430 6530 8.82E+03 η*_(0.l) /η*₁₀₀ — 6.1 3.6 9.2 16.9 Mw daltons 74,000 203,600 322,300 — Mz daltons 182,200 434,500 927,800 — Mw/Mn — 4.3 5.4 7.2 — Mz/Mw — 2.5 2.1 2.9 — IV (Vis) dl/g 0.92 1.05 1.48 — g′ — 0.79 0.92 0.99 — LCBI — 0.52 0.11 0.09 —

Dynamic oscillatory data generated based on analysis of Examples 19-24 are shown in TABLE 7 below. The data in TABLE 7 show that complex viscosity decreases as frequency increases for Examples 11-16. TABLE 3 further shows that visbroken blends of HDPE and PP in Examples 20-22 have a lower complex viscosity (η*) for all tested values of frequency.

TABLE 7 Example 19 20 21 Frequency η* Frequency η* Frequency η* rad/sec poise rad/sec poise rad/sec poise 3.98E+02 2.11E+03 3.98E+02 2.27E+03 3.98E+02 2.30E+03 2.51E+02 2.55E+03 2.51E+02 2.78E+03 2.51E+02 2.82E+03 1.58E+02 3.01E+03 1.58E+02 3.32E+03 1.58E+02 3.39E+03 1.00E+02 3.55E+03 1.00E+02 3.94E+03 1.00E+02 4.04E+03 6.31E+01 4.16E+03 6.31E+01 4.66E+03 6.31E+01 4.79E+03 3.98E+01 4.87E+03 3.98E+01 5.47E+03 3.98E+01 5.63E+03 2.51E+01 5.61E+03 2.51E+01 6.41E+03 2.51E+01 6.61E+03 1.58E+01 6.42E+03 1.58E+01 7.42E+03 1.58E+01 7.65E+03 1.00E+01 7.25E+03 1.00E+01 8.50E+03 1.00E+01 8.77E+03 6.31E+00 8.09E+03 6.31E+00 9.63E+03 6.31E+00 9.96E+03 3.98E+00 8.89E+03 3.98E+00 1.07E+04 3.98E+00 1.11E+04 2.51E+00 9.66E+03 2.51E+00 1.19E+04 2.51E+00 1.24E+04 1.58E+00 1.04E+04 1.58E+00 1.29E+04 1.58E+00 1.36E+04 1.00E+00 1.10E+04 1.00E+00 1.39E+04 1.00E+00 1.48E+04 6.31E−01 1.15E+04 6.31E−01 1.48E+04 6.31E−01 1.58E+04 3.98E−01 1.19E+04 3.98E−01 1.55E+04 3.98E−01 1.68E+04 2.51E−01 1.22E+04 2.51E−01 1.60E+04 2.51E−01 1.75E+04 1.58E−01 1.24E+04 1.58E−01 1.64E+04 1.58E−01 1.80E+04 1.00E−01 1.25E+04 1.00E−01 1.66E+04 1.00E−01 1.83E+04 6.31E−02 1.25E+04 6.31E−02 1.67E+04 6.31E−02 1.85E+04 3.98E−02 1.26E+04 3.98E−02 1.68E+04 3.98E−02 1.86E+04 2.51E−02 1.25E+04 2.51E−02 1.68E+04 2.51E−02 1.87E+04 Example 22 23 24 Frequency η* Frequency η* Frequency η* rad/sec poise rad/sec poise rad/sec poise 3.98E+02 2.20E+03 3.98E+02 1.69E+03 3.98E+02 3.48E+03 2.51E+02 2.72E+03 2.51E+02 2.11E+03 2.51E+02 4.82E+03 1.58E+02 3.28E+03 1.58E+02 2.50E+03 1.58E+02 6.53E+03 1.00E+02 3.94E+03 1.00E+02 2.96E+03 1.00E+02 8.68E+03 6.31E+01 4.69E+03 6.31E+01 3.48E+03 6.31E+01 1.14E+04 3.98E+01 5.55E+03 3.98E+01 4.07E+03 3.98E+01 1.48E+04 2.51E+01 6.54E+03 2.51E+01 4.67E+03 2.51E+01 1.89E+04 1.58E+01 7.59E+03 1.58E+01 5.23E+03 1.58E+01 2.39E+04 1.00E+01 8.73E+03 1.00E+01 5.73E+03 1.00E+01 2.96E+04 6.31E+00 9.94E+03 6.31E+00 6.12E+03 6.31E+00 3.61E+04 3.98E+00 1.12E+04 3.98E+00 6.43E+03 3.98E+00 4.34E+04 2.51E+00 1.24E+04 2.51E+00 6.65E+03 2.51E+00 5.10E+04 1.58E+00 1.37E+04 1.58E+00 6.80E+03 1.58E+00 5.90E+04 1.00E+00 1.50E+04 1.00E+00 6.91E+03 1.00E+00 6.70E+04 6.31E−01 1.63E+04 6.31E−01 6.97E+03 6.31E−01 7.51E+04 3.98E−01 1.76E+04 3.98E−01 7.02E+03 3.98E−01 8.27E+04 2.51E−01 1.87E+04 2.51E−01 7.05E+03 2.51E−01 9.03E+04 1.58E−01 1.95E+04 1.58E−01 7.06E+03 1.58E−01 9.73E+04 1.00E−01 2.01E+04 — — 1.00E−01 1.03E+05 6.31E−02 2.05E+04 — — 6.31E−02 1.08E+05 3.98E−02 2.07E+04 — — 3.98E−02 1.12E+05 2.51E−02 2.08E+04 — — 2.51E−02 1.15E+05

For the sake of brevity, only certain ranges are explicitly disclosed herein. However, in addition to recited ranges, any lower limit may be combined with any upper limit to recite a range not explicitly recited, as well as, ranges from any lower limit may be combined with any other lower limit to recite a range not explicitly recited, in the same way, ranges from any upper limit may be combined with any other upper limit to recite a range not explicitly recited. Additionally, within a range includes every point or individual value between its end points even though not explicitly recited. Thus, every point or individual value may serve as its own lower or upper limit combined with any other point or individual value or any other lower or upper limit, to recite a range not explicitly recited.

Although the present invention and its advantages have been described in detail, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims. Moreover, the scope of the present application is not intended to be limited to the particular embodiments of the processes, machines, film structures, composition of layers, means, methods, and/or steps described in the specification. As one of the ordinary skill in the art will readily appreciate from the disclosure of the present invention, processes, machines, film structures, composition of layers, means, methods, and/or steps, presently existing or later to be developed that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein, may be utilized according to the present invention. Accordingly, the appended claims are intended to include within their scope such processes, machines, film structures, composition of layers, means, methods, and/or steps. 

What is claimed is:
 1. A method for processing polyolefin recyclate comprising: a. providing a polyolefin feedstock having: i) a first density in the range of from 0.900 g/cm³ to 0.970 g/cm³; ii) a first melt index (I₂) less than or equal to 5.0 g/10 min.; iii) a first molecular weight distribution (M_(w)/M_(n)) greater than 4.0; iv) a first weight average molecular weight (“M_(w1)”) greater than or equal to 85,000 daltons; and v) a first melt elasticity (“ER”) greater than or equal to 0.5; b. adding the polyolefin recyclate to a first extruder to produce a first polyolefin recyclate melt; and c. subjecting the first polyolefin recyclate melt to visbreaking conditions to produce a second polyolefin melt having: i) a second density, wherein the ratio of the second density to the first density is greater than or equal to 1.0; ii) a second melt index (I₂), wherein the ratio of the second melt index to the first melt index is greater than or equal to 5.0; iii) a second molecular weight distribution, wherein the ratio of second molecular weight distribution to the first molecular weight distribution is less than or equal to 0.99; iv) a second weight average molecular weight (“M_(w2)”), wherein M_(w2)/M_(w1) is less than or equal to 0.99; and v) a second melt elasticity, wherein the ratio of the second melt elasticity to the first melt elasticity is less than or equal to 0.90.
 2. The method of claim 1, wherein the polyolefin feedstock comprises post-consumer recycled waste, post-industrial recycled waste, or a combination thereof.
 3. The method of claim 1, wherein the visbreaking conditions consist of thermal visbreaking.
 4. The method of claim 3, wherein thermal visbreaking is performed at a temperature greater than or equal to 300° C.
 5. The method of claim 1, further comprise further subjecting the first polyolefin melt to devolatilization conditions to produce the second polyolefin recyclate melt wherein: the polyolefin recyclate feedstock has a first volatile organic compound content; the first polyolefin recyclate melt has a second volatile organic compound content; and the ratio of the second volatile organic compound content to the first volatile organic compound content is less than or equal to 0.9.
 6. The method of claim 5, wherein devolatilization conditions comprise injection and withdrawal of a scavenging gas.
 7. The method of claim 1, wherein the method is characterized by one or more of the following: i) the polyolefin recyclate feedstock have a first high load melt index (I₂₁), the second polyolefin recyclate melt has a second high load melt index, and the ratio of the second high load melt index to the first high load melt index is greater than or equal to 2.0; ii) the polyolefin recyclate feedstock have a first melt index ratio (I₂₁/I₂), the second polyolefin recyclate melt has a second melt index ratio, and the ratio of the second melt index ratio to the first melt index ratio is in the range of 0.30 to 0.60; iii) the polyolefin recyclate feedstock have a first long chain branching parameter (g′) the second polyolefin recyclate melt has a second g′, and the ratio of the second g′ to the first g′ is less than to 1.0, and/or the first g′ is in the range from 0.70 to 0.99; iv) the polyolefin recyclate feedstock have a first long chain branching index (“LCBI”) greater than or equal to 0.60, the second polyolefin recyclate melt has a second LCBI, and the ratio of the second LCBI to the first LCBI is less than or equal to 0.40; v) a first overall polydispersity measure (“PDR”), the second polyolefin recyclate melt has a second PDR, and the ratio of the second PDR to the first PDR is less than or equal to 0.50; vi) the polyolefin recyclate feedstock have a first complex viscosity ratio, the second polyolefin recyclate melt has a second complex viscosity ratio, and the ratio of the second complex viscosity ratio to the first complex viscosity ratio is less than or equal to 0.50, and/or the second complex viscosity ratio is less than or equal to 10; and vii) the polyolefin recyclate feedstock have a first intrinsic viscosity, the second polyolefin recyclate melt has a second intrinsic viscosity, and the ratio of the second intrinsic viscosity to the first intrinsic viscosity is less than or equal to 0.90.
 8. The method of claim 1, wherein a polyolefin recyclate product is formed by withdrawal of the second polyolefin recyclate melt from the first extruder for further processing or pelletizing of the second polyolefin recyclate melt.
 9. The method of claim 8, further comprising: adding the polyolefin recyclate product and a first polyolefin blend component to a second extruder; and effecting compounding conditions in the second extruder to form a polyolefin product comprising the melt-blended mixture of the processed polyolefin recyclate product and the first polyolefin blend component.
 10. The method of claim 9, wherein the first polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof.
 11. The composition of claim 10, wherein: a. the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof; b. the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof; and c. the processed polyolefin recyclate comprises a second processed LDPE recyclate, a second processed LLDPE recyclate, a second processed HDPE recyclate, a second processed MDPE recyclate, a second processed polypropylene recyclate, or a combination thereof.
 12. The method of claim 11, wherein the first polyolefin blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof.
 13. The method of claim 9, wherein the polyolefin recyclate product is added in an amount in the range of from 5 wt. % to 90 wt. % based on the combined weight of the polyolefin recyclate product and the first polyolefin blend component.
 14. The method of claim 9, wherein the compounding conditions include a temperature less than or equal to 300° C.
 15. The method of claim 9, further comprising: adding a second polyolefin blend component to a third extruder; effecting melt conditions in the third extruder to produce a second polyolefin blend component melt; and withdrawing the second polyolefin blend component melt as the first polyolefin blend component.
 16. The method of claim 15, wherein the second blend component comprises a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof.
 17. A composition comprising a polymer blend of: a. a first polymer, wherein the first polymer: i) is a first processed polyolefin recyclate; and ii) is present in an amount in the range of from 5 wt. % to 90 wt. %; and b. a second polymer, wherein the second polymer: i) is a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof; and ii) is present in an amount in the range of from 10 wt. % to 95 wt. %; wherein all weight percentages are based on the combined weight of the first and second polymers.
 18. The composition of claim 17, wherein: a. the virgin polyolefin comprises a virgin LDPE, a virgin LLDPE, a virgin HDPE, a virgin MDPE, a virgin polypropylene, or a combination thereof; b. the polyolefin recyclate feedstock comprises a LDPE recyclate feedstock, a LLDPE recyclate feedstock, a HDPE recyclate feedstock, a MDPE recyclate feedstock, a polypropylene recyclate feedstock, or a combination thereof; and c. the processed polyolefin recyclate comprises a processed LDPE recyclate, a processed LLDPE recyclate, a processed HDPE recyclate, a processed MDPE recyclate, a processed polypropylene recyclate, or a combination thereof.
 19. The composition of claim 17, wherein processed means subjected to thermal visbreaking and optionally subjected to devolatilization.
 20. A blend comprising: a visbroken polyolefin, having a first 12; and a virgin polyolefin, a polyolefin recyclate feedstock, a processed polyolefin recyclate, or a combination thereof, having a second I₂; wherein: ${\log\left( \left( I_{2} \right)_{blend} \right)} = {\sum\limits_{i = 1}^{n}\left( {w_{i} \times {\log\left( \left( I_{2} \right)_{i} \right)}} \right)}$ (I₂)_(blend) is the target melt index of the final blend product; n is the number of components in the blend; and i is the i-th component of an n-component blend. 